TWI768565B - Steam generator, exhaust heat recovery plant, compound plant, steam-electricity cogeneration plant - Google Patents

Abstract

Provided are a steam generating device and an exhaust heat recovery plant.

The steam generating device is provided with: a heat medium flow path for the heat medium to flow; a first carbon block arranged in the heat medium flow path; The second carbon section on the upstream side of the boiler; the first evaporator installed on the upstream side of the second carbon section in the flow direction of the heat medium in the heat medium flow path; the first flash for generating flash steam A steaming tank; a first water supply pipeline formed in such a way as to supply the water heated by the 1st charcoal device to the 2nd charcoal device; The second water supply line constituted by the method of supplying water to the heat utilization equipment.

Description

Steam generator, exhaust heat recovery plant, compound plant, steam-electricity cogeneration plant

The present invention relates to a steam generating device, an exhaust heat recovery plant, a composite plant, a steam-electricity co-generation plant, a transformation method for an exhaust heat recovery plant, and a steam generation method.

Patent Document 1 discloses a method of heating the feed water supplied to the carbon economizer by using the heat of the exhaust gas (heat medium) of the gas turbine, and supplying a part of the feed water from the economizer to the evaporator to the flasher. Evaporation tank (flash evaporator), which is used to generate flash steam from the flash tank. According to this configuration, steam can be generated by utilizing the heat of the relatively low-temperature exhaust gas passing through the carbon economizer, and the heat utilization efficiency of the exhaust gas can be improved.

[Prior Art Literature]

[Patent Document 1] Japanese Patent Laid-Open No. 2019-44678

According to the configuration described in Patent Document 1, and no flash evaporation is provided Compared with the case of the tank, the flow rate of the feed water supplied to the carbon economizer increases according to the flow rate of the feed water supplied to the flash tank. Therefore, in order to make the temperature of the feed water supplied to the carbon economizer close to the saturated steam temperature, a carbon economizer is necessary. size increases. The same is true for a system without a flash tank, and in a system in which a part of the feed water from the carbon economizer to the evaporator is supplied to the heat utilization facility and used as a heat source, similarly, in order to make the water supply to the economizer to be used as a heat source The temperature of the feed water is close to the saturated steam temperature, and the size of the carbon economizer becomes larger if necessary.

In view of the above-mentioned circumstances, an object of the present invention is to provide a steam generator capable of suppressing an increase in the size of a carbon economizer and improving the heat utilization efficiency of a heat medium, and an exhaust heat recovery plant equipped with the steam generator.

The steam generator of the present invention is provided with: a heat medium flow path for the flow of the heat medium; a first carbon block provided in the heat medium flow path; The second carbon separator on the upstream side of the first carbon separator; the first evaporator provided on the upstream side of the second carbon separator in the flow direction of the heat medium in the heat medium flow path; The first water supply pipeline constituted by the way of supplying the water heated by the aforementioned first section of the carbon device to the aforementioned second section of the carbon device; The second water supply constituted by the method of supplying water to the heat utilization equipment pipeline.

According to the present invention, there are provided a steam generator capable of suppressing an increase in the size of a carbon economizer, and also capable of improving the heat utilization efficiency of a heat medium, and an exhaust heat recovery plant provided with the steam generator.

2: Compound Factory

4: Gas Turbine

5: Exhaust heat recovery boiler

6(6A~6D): Steam generating device

8(8a~8d): Flash tank

9: Chimney

12,140: Compressor

14: Burner

16: Turbine

18: Exhaust gas flow path

19: Generator

20, 116, 120, 122, 124: Heat Exchangers

126, 128, 129, 130, 132: Heat Exchangers

21,48: Water supply lines

22: 1st low pressure carbon saver

23: Low temperature heat exchanger

24: 2nd low pressure carbon saver

25: 3rd low pressure carbon saver

26: Low pressure evaporator

27, 29, 48, 52, 53, 54, 60: Water supply lines

63,64,70,73,74,75,76,77,79: Water supply lines

28: Low pressure superheater

30: 1st high pressure carbon saver

31: Medium pressure carbon saver

32: Medium pressure evaporator

34: Medium pressure superheater

36: 2nd high pressure carbon saver

38: High pressure evaporator

40: 1st high pressure superheater

42: 1st reheater

44: 2nd high pressure superheater

46: 2nd reheater

50: Condensate pump

51: Condensate line

55, 65, 77: Feed valve

56, 57, 58, 66, 68, 78, 80: Vapor Lines

86, 92, 93, 94, 95, 97, 117, 118: Vapor Lines

59,84,85,86,87: Pressure reducing valve

61: Feed water pump

62: Medium pressure feed pump

69,88,89,90,91: Superheater

71: Drain water line

72: High pressure feed pump

81,83: Desuperheater

82,98: Reheat steam lines

96: Low pressure carbon economizer

100: Steam Turbine Systems

102: High Pressure Steam Turbines

104: Intermediate pressure steam turbines

106: Low Pressure Steam Turbines

108: Condenser

110: Medium pressure exhaust line

112: Low pressure exhaust line

114: High pressure exhaust line

119: Valve

126: Cooling Media Cooler

127: Bearings

128: Lube oil cooler

134: Air line for cooling

136, 138: Extraction line

142: Low Boiling Media Blue Gold Cycle

200: Exhaust heat recovery plant

205, 206: Flow adjustment valve

1 is a diagram showing a schematic overall configuration of a composite factory 2 ( 2A) according to an embodiment.

[ Fig. 2 ] A line showing the relationship between the heat quantity and temperature of the feed water from the carbon economizer to the first evaporator of the steam generator, and the relationship between the heat quantity and temperature of the exhaust gas from the first evaporator to the carbon economizer The graph of the line is a graph relating to a steam generator (Comparative Example 1) provided with only one carbon economizer but not provided with a flash tank.

[ Fig. 3 ] A line showing the relationship between the heat quantity and temperature of the feed water from the carbon economizer to the first evaporator of the steam generator, and the relationship between the heat quantity and temperature of the exhaust gas from the first evaporator to the carbon economizer Figure 3 is about a steam generator that only has one carbon economizer and a flash tank, and uses the flash tank to flash the water at the inlet of the first evaporator to recover the ideal maximum heat. (Comparative Example 2).

[ Fig. 4 ] A line showing the relationship between the heat quantity and temperature of the feed water from the carbon economizer to the first evaporator of the steam generator, and from the first evaporator to the carbon economizer The graph of the relationship between the heat of the exhaust gas and the temperature, and the relationship is related to only one carbon economizer and a flash tank, and approaching the temperature difference (saturation temperature under the pressure of the first evaporator and the first evaporator A diagram of a steam generator (Comparative Example 3) in which the difference in feed water temperature at the inlet of the device) is not zero.

[ Fig. 5 ] A line showing the relationship between the heat quantity and temperature of the feed water from the carbon economizer to the first evaporator of the steam generator, and the relationship between the heat quantity and temperature of the exhaust gas from the first evaporator to the carbon economizer The diagram of the line is a diagram related to the steam generator 6 of the embodiment including the first carbonizer, the second carbonizer, and the flash tank.

[ Fig. 6] Fig. 6 is a diagram showing a schematic overall configuration of a composite factory 2 (2B) according to another embodiment.

[ Fig. 7] Fig. 7 is a diagram showing a schematic overall configuration of a composite factory 2 (2C) according to another embodiment.

[ Fig. 8] Fig. 8 is a diagram showing a schematic overall configuration of a composite factory 2 (2D) according to another embodiment.

[ Fig. 9] Fig. 9 is a diagram showing a schematic overall configuration of a composite factory 2 (2B) according to another embodiment.

10 is a diagram showing a schematic overall configuration of a composite factory 2 (2D) according to another embodiment.

11 is a diagram showing a schematic overall configuration of a composite factory 2 ( 2E) according to another embodiment.

12 is a diagram showing a schematic overall configuration of a composite factory 2 ( 2E) according to another embodiment.

[ Fig. 13 ] shows the steam generator from the low temperature heat exchanger to the first A graph showing the relationship between the heat and temperature of the feed water of the evaporator, and the relationship between the heat and temperature of the exhaust gas from the first evaporator to the low-temperature heat exchanger, and the relationship is related to a low-temperature heat exchanger, A diagram of the steam generator 6 of the embodiment of the first carbonizer, the second carbonizer, the third carbonizer, and the flash tank.

Hereinafter, some embodiments will be described with the accompanying drawings. The dimensions, materials, shapes, relative arrangements, etc. of the components described in the embodiments or shown in the drawings are not intended to limit the scope of the invention, but are merely illustrative examples.

For example, expressions indicating relative or absolute arrangement such as "in a certain direction", "along a certain direction", "parallel", "orthogonal", "center", "concentric" or "coaxial" are strictly It does not mean only the arrangement like this description, but also means the state of relative displacement by tolerance, or angle or distance to the extent that the same function can be obtained.

For example, expressions such as "identical," "equal," and "homogeneous" denote the state of equality of things. Strictly speaking, they do not only denote the state of equality, but also denote the state of the existence of tolerance, or the state of difference in the degree of obtaining the same function. .

For example, the expression indicating a shape such as a square shape or a cylindrical shape does not only indicate a shape such as a square shape or a cylindrical shape in the strict sense of geometry, but also indicates that the concavo-convex part or the inverted part is included within the range where the same effect can be obtained. shape of corners, etc.

On the other hand, the expression "includes", "has", "has", "includes", or "includes" a constituent element is not an exclusive expression that excludes the existence of other constituent elements.

<Configuration of the compound factory>

FIG. 1 is a diagram showing a schematic overall configuration of a composite factory 2 ( 2A) according to an embodiment. .

The compound plant 2 includes a gas turbine 4 as a prime mover, a steam turbine system 100 , a steam generator 6 ( 6A) that generates steam including an exhaust heat recovery boiler 5 , and discharges exhaust gas discharged from the exhaust heat recovery boiler 5 To Atmospheric Chimney 9. The steam turbine system 100 functions as a steam utilization facility that utilizes the steam generated by the steam generator 6 . Further, the steam generator 6 and the steam turbine system 100 constitute an exhaust heat recovery plant 200 for recovering the exhaust heat of the gas turbine 4 .

<Configuration of gas turbine>

The gas turbine 4 includes a compressor 12 that compresses air, a combustor 14 that combusts fuel using the compressed air generated by the compressor 12 , and a turbine 16 that is driven by the combustion air generated by the combustor 14 . In the form shown in the figure, the generator 19 is arranged on the same axis as the compressor 12 and the turbine 16, and the rotors of the compressor 12, the turbine 16, and the generator 19 are configured to rotate integrally.

<Configuration of steam turbine system>

The steam turbine system 100 includes a plurality of steam turbines 102 , 104 , and 106 , and a condenser 108 that cools the steam discharged from the steam turbine 106 and returns it to water. The steam turbine system 100 includes a high pressure steam turbine 102, an intermediate pressure steam turbine 104, and a low pressure steam turbine 106 as a plurality of steam turbines. The vapor outlet of the intermediate pressure steam turbine 104 and the vapor inlet of the low pressure steam turbine 106 are connected via an intermediate pressure exhaust line 110 , and the vapor outlet of the low pressure steam turbine 106 and the condenser 108 are connected via a low pressure exhaust line 112 . In the illustrated form, the compressor 12, the turbine 16, the generator 19, the high pressure steam turbine 102, the intermediate pressure steam turbine 104, and the low pressure steam turbine 106 are arranged on the same axis, and the rotors are configured to rotate integrally.

<Configuration of steam generator>

The steam generator 6 ( 6A) includes the exhaust heat recovery boiler 5 to which the exhaust gas (heat medium) of the gas turbine 4 is supplied, and the flash tank 8 as the first flash tank. In addition, the flash tank 8 is also a heat utilization facility that receives the supply of heated water and generates steam by using the heat of the water.

The exhaust heat recovery boiler 5 includes an exhaust gas flow path 18 (heat medium flow path) through which the exhaust gas of the gas turbine 4 flows, and a plurality of heat exchangers 20 provided in the exhaust gas flow path 18 . The plurality of heat exchangers 20 include a first low-pressure carbon economizer 22 (first carbon economizer) and a second low-pressure economizer 24 in order from the downstream side in the flow direction of the exhaust gas in the exhaust gas flow path 18 (2nd carbon economizer), low pressure evaporator 26 (1st evaporator), low pressure superheater 28, first high pressure economizer 30, medium pressure evaporator 32, medium pressure superheater 34, second high pressure economizer boiler 36 , high pressure evaporator 38 , first high pressure superheater 40 , first reheater 42 , second high pressure superheater 44 , and second reheater 46 . In the flow direction of the exhaust gas in the exhaust gas flow path 18 , the second low-pressure economizer 24 is located upstream of the first low-pressure economizer, and the low-pressure evaporator 26 is located upstream of the second low-pressure economizer 24 . side. Between the low-pressure superheater 28 and the intermediate-pressure evaporator 32 in the exhaust gas flow path 18 , the intermediate-pressure economizer 31 and the first high-pressure economizer 30 are arranged in parallel.

The condenser 108 and the first low pressure economizer 22 are connected via a water supply line 48 , and the water supply line 48 is provided with a condensate water pump 50 for supplying the condensed water from the condenser 108 to the first low pressure economizer 22 .

The first low pressure economizer 22 heats the water supplied from the water supply line 48 by heat exchange with the exhaust gas. A part of the water heated by the first low pressure economizer 22 is supplied to the second low pressure economizer 24 via the water supply line 52 connecting the first low pressure economizer 22 and the second low pressure economizer 24 .

The flash tank 8 is connected to a water supply line 53 branched from the water supply line 52 , and a part of the water heated by the first low-pressure carbon economizer 22 is supplied to the flash tank 8 via the water supply line 53 . The water supply line 53 is provided with a pressure reducing valve 59 for reducing the pressure of the heating water supplied from the first low-pressure carbon economizer 22 . The heated water supplied to the flash tank 8 via the water supply line 53 is decompressed in the flash tank 8 and evaporated (flashed) to become flash vapor. The flash steam generated by the flash tank 8 is supplied to the middle section of the low pressure steam turbine 106 via a steam line 57 connecting the flash tank 8 and the middle section of the low pressure steam turbine 106 .

The condensed water accumulated at the bottom of the flash tank 8 is The condensed water line 51 connected to the flash tank 8 and the water supply line 48 flows into the water supply line 48 , and is supplied to the first low-pressure carbon economizer 22 via the water supply line 48 . A feed water pump 61 is provided on the condensed water line 51 , and the condensed water system discharged from the flash tank 8 is sent to the first low-pressure carbon economizer 22 by pressure via the feed water pump 61 . The condensed water (eg 90°C) discharged from the flash tank 8 is higher temperature than the water flowing in the water supply line 48 (eg 35°C), and the water flowing in the water supply line 48 is combined with the condensed water discharged from the flash tank 8 After mixing, the temperature rises to the feed water temperature (for example, 60° C.) at the inlet of the first low-pressure carbon economizer 22 . As a result, the temperature of the feed water at the inlet of the first low-pressure economizer 22 is ensured to be higher than the dew point temperature of the exhaust gas, so that condensation of moisture in the exhaust gas in the first low-pressure economizer 22 can be prevented. In the case where the first low-pressure carbon saver 22 is made of a relatively inexpensive material, corrosion can still be prevented.

In this example, a part of the water heated by the first low-pressure carbon economizer 22 is supplied to the flash tank 8 via the feed water line 53 . A portion of the water supplied by the feed water line 53 is evaporated from the flash tank 8 and used for the drive of the low pressure steam turbine 106, while the other portion is mixed with the water flowing in the feed water line 48 as condensed water for use in the feed water. Heating of water flowing in line 48. That is, the condensed water line 51 and the water supply pump 61 are configured to flow in the water supply line 48 by mixing the water flowing in the water supply line 48 with the condensed water having a high temperature from the water supplied from the water supply line 53. The heat utilization equipment for heating the water, the flash tank 8 and the low-pressure steam turbine 106 constitute a power generation device that uses the water supplied from the water supply line 53 as a heat source to generate power.

Generally speaking, it will be a low pressure evaporation of 140℃~180℃ The feed water at the inlet of the evaporator 26 (the first evaporator) is mixed with the water flowing in the feed water line 48 for heating, and heat of a high temperature higher than necessary is eventually used, and the heat utilization efficiency is low. The temperature rise of the water flowing in the water supply line 48 can be effectively achieved by using the heated water from the outlet of the first low pressure economizer 22 with the feed water at the inlet of the lower pressure evaporator 26 (the first evaporator) being low temperature. By utilizing low-temperature heat to heat the intake air, the heat utilization efficiency can be improved. Heat at a temperature of more than 100°C can generate water vapor at normal pressure, and heat at a temperature of more than 100°C is significantly different from that below 100°C.

Therefore, if the feed water at the inlet of the low-pressure evaporator 26 (first evaporator) at 140°C to 180°C is mixed with the heating medium having a heat of 100°C or less, which is of low utility value, and the heating medium is heated, the water will be heated. Significant loss of heat utilization value. Conversely, if the heated water at the outlet of the first low-pressure carbon economizer 22 whose inlet water temperature is low in the lower-pressure evaporator 26 (first evaporator) is used to heat the heated medium below 100°C, there will be no significant losses. The utilization value of heat can be improved, and the heat utilization efficiency can be improved. In this embodiment, the heating water at the outlet of the first low-pressure carbon economizer 22 is flashed to obtain steam, and the remaining lower-temperature condensed water is mixed with the medium to be heated for heating, which can further improve the heat utilization efficiency .

The second low pressure economizer 24 heats the water supplied from the first low pressure economizer 22 via the water supply line 52 by heat exchange with the exhaust gas. A part of the water heated by the second low-pressure carbon economizer 24 is supplied to the low-pressure evaporator 26 via the water supply line 54 connecting the second low-pressure economizer 24 and the low-pressure evaporator 26 .

The low pressure evaporator 26 will pass from the second low pressure economizer 24 through The water supplied from the water supply line 54 is heated and evaporated by heat exchange with the exhaust gas, thereby generating low-pressure steam. The water supply line 54 is provided with a water supply valve 55 for decompressing the water supplied from the second low-pressure carbon economizer 24 . A portion of the low pressure vapor produced by the low pressure evaporator 26 is supplied to the low pressure superheater 28 via a vapor line 56 connecting the low pressure evaporator 26 and the low pressure superheater 28 .

The low pressure superheater 28 superheats the low pressure steam supplied from the low pressure evaporator 26 via the steam line 56 by heat exchange with the exhaust gas to generate low pressure superheated steam. The low pressure superheated steam produced by the low pressure superheater 28 flows into the medium pressure exhaust line 110 through the steam line 58 connecting the low pressure superheater 28 to the medium pressure exhaust line 110, and from the medium pressure exhaust line 110 into the low pressure steam turbine 106 steam inlet.

A part of the water heated by the second low pressure economizer 24 is supplied to the medium pressure economizer 31 via the water supply line 60 . The water supply line 60 is branched from the water supply line 54 and is connected to the medium-pressure carbon economizer 31 . The heating water flowing in the water supply line 60 is sent to the medium pressure carbon economizer 31 under pressure by the medium pressure water supply pump 62 provided on the water supply line 60 .

The medium pressure economizer 318 heats the water supplied from the second low pressure economizer 24 through the water supply line 60 by heat exchange with the exhaust gas. The water heated by the medium pressure carbon economizer 31 is supplied to the medium pressure evaporator 32 through the water supply line 64 connecting the medium pressure carbon economizer 31 and the medium pressure evaporator 32 .

The medium-pressure evaporator 32 heats and evaporates the water supplied from the medium-pressure carbon economizer 31 through the water supply line 64 through heat exchange with the exhaust gas, thereby generating medium-pressure steam. The water supply line 64 is provided with a water supply valve 65 for decompressing the water supplied from the medium-pressure carbon economizer 31 . Produced by the medium pressure evaporator 32 A portion of the pressure steam is supplied to the intermediate pressure superheater 34 via a steam line 66 connecting the intermediate pressure evaporator 32 and the intermediate pressure superheater 34 .

The intermediate pressure superheater 34 superheats the intermediate pressure steam supplied from the intermediate pressure evaporator 32 through the steam line 66 by heat exchange with the exhaust gas to generate intermediate pressure superheated steam. The intermediate pressure superheated steam generated by the intermediate pressure superheater 34 is supplied via the steam line 68 to the high pressure exhaust line 114 connecting the steam outlet of the high pressure steam turbine 102 and the steam inlet of the first reheater 42 . The intermediate-pressure superheated steam generated by the intermediate-pressure superheater 34 flows into the first reheater 42 via the steam line 68 and the high-pressure exhaust line 114 .

A part of the water heated by the second low pressure economizer 24 is supplied to the first high pressure economizer 30 via the water supply line 70 connecting the second low pressure economizer 24 and the first high pressure economizer 30 . The heating water flowing in the water supply line 70 is sent to the first high-pressure carbon economizer 30 under pressure by the high-pressure water supply pump 72 provided in the water supply line 70 .

The first high pressure economizer 30 heats the heating water supplied from the second low pressure economizer 24 through the water supply line 70 by heat exchange with the exhaust gas. The heated water heated by the first high-pressure carbon economizer 30 is supplied to the second high-pressure economizer 36 through the water supply line 74 connecting the first high-pressure economizer 30 and the second high-pressure economizer 36 .

The second high-pressure economizer 36 heats the high-pressure heating water supplied from the first high-pressure economizer 30 via the water supply line 74 by heat exchange with the exhaust gas. The high-pressure heating water heated by the second high-pressure carbon economizer 36 is supplied to the high-pressure evaporator 38 through the water supply line 76 connecting the second high-pressure economizer 36 and the high-pressure evaporator 38 .

The high-pressure evaporator 38 heats and evaporates the water supplied from the second high-pressure carbon economizer 36 through the water supply line 76 by heat exchange with the exhaust gas, thereby generating high-pressure steam. The water supply line 76 is provided with a water supply valve 77 for decompressing the water supplied from the second high-pressure carbon economizer 36 . The high-pressure steam generated by the high-pressure evaporator 38 is supplied to the first high-pressure superheater 40 through a steam line 78 connecting the high-pressure evaporator 38 and the first high-pressure superheater 40 .

The first high-pressure superheater 40 superheats the high-pressure steam supplied from the high-pressure evaporator 38 through the steam line 78 by heat exchange with the exhaust gas to generate high-pressure superheated steam. The high-pressure superheated steam generated by the first high-pressure superheater 40 is supplied to the second high-pressure superheater 44 through the steam line 80 connecting the first high-pressure superheater 40 and the second high-pressure superheater 44 . The steam line 80 is provided with a desuperheater 81 for reducing the temperature of the high-pressure superheated steam flowing in the steam line 80 .

The second high-pressure superheater 44 further superheats the high-pressure superheated steam supplied from the first high-pressure superheater 40 through the steam line 80 by heat exchange with the exhaust gas. The high-pressure superheated steam superheated by the second high-pressure superheater 44 is supplied to the high-pressure steam turbine 102 through a steam line 97 connecting the second high-pressure superheater 44 and the steam inlet of the high-pressure steam turbine 102 .

The first reheater 42 supplies the steam from the steam outlet of the high pressure steam turbine 102 to the first reheater 42 via the high pressure exhaust line 114 and from the intermediate pressure superheater 34 through the steam line 68 and the high pressure exhaust line 114 The steam to the first reheater 42 is superheated by heat exchange with the exhaust gas. The steam superheated by the first reheater 42 is supplied to the second reheater 46 through the steam line 82 connecting the first reheater 42 and the second reheater 46 . steam pipe On line 82, a desuperheater 83 for desuperheating the vapor flowing in vapor line 82 is provided.

The second reheater 46 superheats the steam supplied through the steam line 82 by heat exchange with the exhaust gas. The steam superheated by the second reheater 46 is supplied to the intermediate pressure steam turbine 104 via a steam line 98 connecting the second reheater 46 and the steam inlet of the intermediate pressure steam turbine 104 .

The effects obtained by the steam generator 6 described above will be described using the TQ diagrams shown in FIGS. 2 to 5 . 2 to 5 are lines showing the relationship between the heat and temperature of the feed water from the carbon economizer to the first evaporator of the steam generator, and the heat and temperature of the exhaust gas from the first evaporator to the carbon economizer diagram of the line of relationships. FIG. 2 is a diagram of a steam generator (Comparative Example 1) provided with only one carbon economizer and not provided with a flash tank. Fig. 3 is a diagram of a steam generator (Comparative Example 2) that has only one carbon economizer and a flash tank, and uses the flash tank to flash the water at the inlet of the first evaporator to recover the ideal maximum heat. picture. Fig. 4 is related to the steam with only one carbon economizer and a flash tank, and the approach temperature difference (the difference between the saturation temperature under the pressure of the first evaporator and the temperature of the feed water at the inlet of the first evaporator) is not zero A graph of the device (Comparative Example 3) was generated. 5 : is a figure which concerns on the steam generator 6 of the said embodiment provided with the 1st carbonizer, the 2nd carbonizer, and the flash tank.

In the examples shown in Fig. 2, Fig. 3 and Fig. 5, in order to improve the heat utilization efficiency, the approximate temperature difference is 0, which means that the water at the inlet of the evaporator is saturated water (the case where the dryness is 0% at the saturated temperature) .

As shown in Fig. 2, in Comparative Example 1, since no flash evaporation was provided Therefore, the heat recovery amount of the exhaust heat recovery boiler 5 is small, and the exhaust gas is released with a high temperature, so the heat utilization efficiency is low.

In addition, as shown in FIG. 3, in the comparative example 2, in the ideal case where the heat recovery amount is maximized and the heat utilization efficiency is increased, the flash flow rate is set so that the gradient of the line representing the water supply and the exhaust gas is set. lines are equal. At this time, the heat recovery amount is large, and the temperature difference between the exhaust gas and the feed water of the carbon economizer is small from the inlet to the outlet, so high heat utilization efficiency can be obtained, but the carbon economizer is large.

In addition, as shown in FIG. 4, in Comparative Example 3, the flash flow rate was set so that the slope of the line representing the feed water was equal to the line of the exhaust gas, so that when the temperature of the feed water at the inlet of the first evaporator was lowered, it was avoided that the The phenomenon that the heat transfer area of the carbon economizer is too large. At this time, although the amount of heat recovered is the same as that shown in FIG. 5 , in the first evaporator, a part of the heat recovered from the exhaust gas is used from the inlet temperature of the first evaporator of the water supply to the temperature of the first evaporator. The increase in the saturation temperature under pressure reduces the amount of heat available for evaporation and reduces the amount of vapor in the first evaporator. Therefore, the flow rate of the flash vapor at low pressure and low temperature increases, while the vapor in the first evaporator, which is higher in pressure and high temperature than the flash vapor and has a higher utility value, is reduced. Therefore, the heat utilization efficiency is higher than that shown in FIG. 5 . low.

On the other hand, the steam generator 6 according to the embodiment shown in FIGS. 1 and 5 is provided with a water supply line 52 for supplying the water heated by the first low-pressure economizer 22 to the second low-pressure economizer 24, and an automatic The heating water line 52 is branched and arranged to supply the water heated by the first low-pressure carbon economizer 22 to the water supply line 53 of the flash tank 8, so the flow rate of the second low-pressure economizer 24 is higher than that of the first low-pressure economizer 22 is less (in Figure 5, the feed water of the second low-pressure carbon economizer The slope of the line becomes larger than the slope of the water supply line of the first low-pressure carbon economizer). Therefore, according to the flow rate of the feed water supplied to the flash tank 8, even if the flow rate of the feed water to the first low pressure economizer 22 increases, the temperature of the feed water can be efficiently approached to saturation by using the smaller second low pressure economizer 24 steam temperature. In addition, in the first low-pressure carbon economizer 22, the temperature difference between the exhaust gas and the feed water is large, so even if the flow rate of the feed water increases, the size can be reduced. Therefore, the size of the carbon economizer (the sum of the size of the first low-pressure economizer 22 and the size of the second low-pressure economizer 24) can be suppressed compared with the case where one economizer is used to bring the temperature of the feed water close to the saturated steam temperature. ), and the flash tank 8 can be used to improve the heat utilization efficiency of the heat medium.

<Variation example of compound factory 2>

Next, a modification example of the composite factory 2 will be described with reference to FIGS. 6 to 12 .

In the composite factory 2 ( 2A to 2F) related to the several embodiments shown in FIGS. 6 to 12 , the symbols that are common to the respective components of the composite factory 2 shown in FIG. 1 are the same as those shown in FIG. 1 unless otherwise specified. Each configuration of the shown steam generator has the same configuration, and the description thereof is omitted.

FIG. 6 is a diagram showing a schematic overall configuration of a composite factory 2 ( 2B) according to another embodiment. FIG. 7 is a diagram showing a schematic overall configuration of a composite factory 2 ( 2C) according to another embodiment.

In some embodiments, for example, as shown in FIGS. 6 and 7 , the steam generator 6 ( 6B, 6C) of the compound plant 2 ( 2B, 2C) is further provided with a steam generator 6 ( 6B, 6C ) for heating the second low-pressure carbon economizer 24 . The water is supplied to the feed water line 63 of the flash tank 8 . The water supply line 63 diverges from the water supply line 54 and is separated from the The water supply lines 53 merge.

Thereby, the flow rate of the second low-pressure economizer 24 can be adjusted, and high efficiency can be obtained with a moderately sized economizer. In addition, it can have an influence on the evaporation amount of the low pressure evaporator 26. In particular, the temperature of the feed water at the outlet of the second low pressure carbon economizer 24, which is important, is kept high (the approach temperature difference of the low pressure evaporator 26 is kept close to 0), and the The temperature difference between the exhaust gas and the feed water of the first carbon economizer 22 is maintained at a constant value larger than that of the water supply outlet of the first carbon economizer 22 . Here, when the temperature difference between the exhaust gas and the feed water is constant, the heat exchange amount is the largest in terms of size. Therefore, the size of the first carbon block 22 can be reasonably miniaturized, and only the The second low-pressure carbon economizer 24, which is particularly important in performance, is increased in size to improve efficiency.

In some embodiments, for example, as shown in FIG. 7 , the steam generator 6 ( 6C) of the compound plant 2 ( 2C) further includes a superheater 69 for superheating the steam generated in the flash tank 8 . The superheater 69 superheats the steam flowing in the steam line 57 by exchanging heat between the heated water flowing in the feed water line 63 and the steam flowing in the steam line 57 . In another embodiment, as shown in FIG. 6 , the heated water flowing in the water supply line 63 can be directly supplied to the flash tank 8 without passing through the superheater 69 .

As shown in FIG. 7 , by superheating the steam flowing in the steam line 57 with the superheater 69 by using the high-temperature feed water flowing in the water supply line 63, the steam at a higher temperature can be used than in the case of not superheated, and the heat utilization efficiency can be improved. . In addition, by making the steam into a superheated state, condensation in the piping such as the steam line 57 can be suppressed, and troubles such as clogging of the piping due to drain water can also be suppressed. Also, the steam from the superheater 69 is used in the steam turbine In this case, the wettability of the downstream section of the steam turbine can be reduced and the corrosion of the turbine airfoils can be suppressed, and the efficiency of the steam turbine can be improved. In particular, by using the feed water obtained from a plurality of locations to generate flash steam, the steam generated by the low-temperature water flash can also be superheated by the high-temperature feed water, and a large amount of high-temperature heating steam can be generated.

In some embodiments, for example, as shown in FIG. 8 , the steam generator 6 ( 6D) of the compound plant 2 ( 2D) further includes a low-temperature heat exchanger 23 and a third low-pressure carbon economizer 25 . In the mode shown in FIG. 8 , the condenser 108 and the low temperature heat exchanger 23 are connected by a water supply line 21 , and the water supply line 21 is provided with a condenser for supplying the condensed water from the condenser 108 to the low temperature heat exchanger 23 water pump 50.

The low temperature heat exchanger 23 heats the water supplied from the water supply line 21 by heat exchange with the exhaust gas. The water heated by the low-temperature heat exchanger 23 is supplied to the first low-pressure carbon economizer 22 via a water supply line 29 connecting the low-temperature heat exchanger 23 and the first low-pressure economizer 22 . In the low-temperature heat exchanger 23, the temperature of the exhaust gas is lowered by the heat exchange with water, and a part of the moisture in the exhaust gas is condensed, and a part of the latent heat released can also be recovered in the water, which can improve the heat utilization efficiency . Since the low-temperature heat exchanger 23 can prevent corrosion caused by condensed water, it can be made of a material such as stainless steel with high corrosion resistance.

The first low-pressure carbon economizer 22 heats the water supplied from the water supply line 29 by heat exchange with the exhaust gas. A part of the water heated by the first low pressure economizer 22 is supplied to the second low pressure economizer 24 via the water supply line 52 connecting the first low pressure economizer 22 and the second low pressure economizer 24 .

A part of the water heated by the second low pressure economizer 24 is supplied to the third low pressure economizer 25 via the water supply line 27 connecting the second low pressure economizer 24 and the third low pressure economizer 25 .

The third low-pressure economizer 25 heats the water supplied from the second low-pressure economizer 24 via the water supply line 27 by exchanging heat with the exhaust gas. A part of the water heated by the third low-pressure carbon economizer 25 is supplied to the low-pressure evaporator 26 via the feed water line 54 connecting the third low-pressure economizer 25 and the low-pressure evaporator 26 .

The low-pressure evaporator 26 heats and evaporates the water supplied from the third low-pressure carbon economizer 25 through the water supply line 54 by heat exchange with the exhaust gas, thereby generating low-pressure steam. The water supply line 54 is provided with a water supply valve 55 for reducing the pressure of the water supplied from the third low-pressure carbon economizer 25 . A portion of the low pressure vapor produced by the low pressure evaporator 26 is supplied to the low pressure superheater 28 via a vapor line 56 connecting the low pressure evaporator 26 and the low pressure superheater 28 .

A part of the water heated by the third low pressure economizer 25 is supplied to the medium pressure economizer 31 via the water supply line 60 . The water supply line 60 is branched from the water supply line 54 and connected to the medium pressure carbon saver 31. The heating water system flowing in the water supply line 60 is sent to the medium pressure carbon saver by the medium pressure water pump 62 provided in the water supply line 60. device 31.

The medium pressure economizer 31 heats the water supplied from the third low pressure economizer 25 via the water supply line 60 by heat exchange with the exhaust gas. The water heated by the medium pressure carbon economizer 31 is supplied to the medium pressure evaporator 32 through the water supply line 64 connecting the medium pressure carbon economizer 31 and the medium pressure evaporator 32 .

In the form shown in FIG. 8, the steam generator 6 (6D) of the compound plant 2 (2D) includes a plurality of flash tanks 8a to 8d whose pressures are set to be different from each other, and the plurality of flash tanks 8a to 8d are connected in series Furthermore, a discharge water line 71 for guiding the discharge water discharged from each of the flash tanks 8a to 8d, and a plurality of water supply lines 73 for supplying the water heated by the exhaust gas from the exhaust heat recovery boiler 5 to the discharge water line 71, 75, 77. The feed water line 73 branches off from the feed water line 54 and is connected to the flash tank 8a. The water supply line 75 is branched from the water supply line 27 and merges at a position between the flash tank 8a and the flash tank 8b of the discharge water line 71 . The water supply line 77 is branched from the water supply line 52 and merges at a position between the flash tank 8b and the flash tank 8c in the discharge water line 71 .

A pressure reducing valve 84 is provided on the water supply line 73 . A pressure reducing valve 85 is provided at a position between the flash tank 8a and the flash tank 8b in the discharge water line 71 . A pressure reducing valve 86 is provided at a position between the flash tank 8b and the flash tank 8c in the discharge water line 71 . A pressure reducing valve 87 is provided at a position between the flash tank 8c and the flash tank 8d in the discharge water line 71 .

The water supply line 79 branched from the water supply line 73 is connected to the position between the flash tank 8c and the flash tank 8d in the discharge water line 71 . On the water supply line 79, a plurality of superheaters 88, 89, 90, 91 are provided.

In the flash tank 8, the heated water supplied from the water supply line 73 is decompressed and evaporated (flashed) to generate flash steam. The flashed vapor produced by flash tank 8a flows into intermediate pressure exhaust line 110 via vapor line 92 connecting flash tank 8a and intermediate pressure exhaust line 110, and into the low pressure steam turbine via intermediate pressure exhaust line 110 106 steam inlet. A superheater 88 is arranged on the steam line 92, and the steam flowing in the steam line 92 is connected to the superheater 88 by It is supplied to the low pressure steam turbine 106 after being superheated by heat exchange with the heating water flowing in the feed water line 79 .

In the flash tank 8b, the drain water discharged from the flash tank 8a and the heated water supplied from the water supply line 75 are decompressed and evaporated (flashed) to generate flash vapor. The flash vapor produced by flash tank 8b flows into low pressure steam turbine 106 via vapor line 93 connecting flash tank 8b to the intermediate section of low pressure steam turbine 106 . The steam line 93 is provided with a superheater 89, and the steam flowing in the steam line 93 is superheated by the superheater 89 by heat exchange with the heating water flowing in the feed water line 79 and then supplied to the low pressure steam turbine 106 .

In the flash tank 8c, the drain water discharged from the flash tank 8b and the heated water supplied from the water supply line 77 are decompressed and evaporated (flashed) to generate flash vapor. Flash vapor produced by flash tank 8c flows into low pressure steam turbine 106 via vapor line 94 connecting flash tank 8c to the intermediate section of low pressure steam turbine 106 . The steam line 94 is provided with a superheater 90, and the steam flowing in the steam line 94 is superheated by the superheater 90 by heat exchange with the heating water flowing in the feed water line 79 and then supplied to the low pressure steam turbine 106 .

In the flash tank 8d, the drain water discharged from the flash tank 8c and the heated water supplied from the water supply line 79 are depressurized and evaporated (flashed) to generate flash vapor. The flash vapor produced by flash tank 8d flows into low pressure steam turbine 106 via vapor line 95 connecting flash tank 8d to the intermediate section of low pressure steam turbine 106 . There is a superheater 91 on the steam line 95, and the steam flowing in the steam line 95 is passed through the superheater 91 and the water supply line 79. The flowing heated water is superheated by heat exchange and then supplied to the low pressure steam turbine 106 .

Here, in the flow direction of the steam in the low-pressure steam turbine 106, the position where the steam line 93 is connected to the low-pressure steam turbine 106 is more downstream than the position where the intermediate-pressure exhaust line 110 is connected to the low-pressure steam turbine 106; the steam line 94 The position connected to the low-pressure steam turbine 106 is further downstream than the position where the steam line 93 is connected to the low-pressure steam turbine 106, and the position where the steam line 95 is connected to the low-pressure steam turbine 106 is more downstream than the position where the steam line 94 is connected to the low-pressure steam turbine 106 more downstream side.

Here, the temperature Tw1 of the water flowing in the water supply line 75 is lower than the saturation temperature Ta, and this saturation temperature Ta is corresponding to the direction of the flow of the discharge water line 71 in the plurality of flash tanks 8a to 8d, which is lower than the discharge water line 71. The connection position P1 of the water line 71 and the water supply line 75 is the pressure Pa of the flash tank 8a on the upstream side. In addition, the temperature Tw1 of the water flowing in the water supply line 75 is higher than the saturation temperature Tb, and this saturation temperature Tb is corresponding to the flow direction of the discharge water line 71 in the plurality of flash tanks 8a to 8d, which is higher than the discharge water line. The connection position P1 between 71 and the feed water line 75 is the pressure Pb of the flash tank 8b on the downstream side.

The temperature Tw2 of the water flowing in the water supply line 77 is lower than the saturation temperature, and this saturation temperature is corresponding to the direction of the flow of the discharge water line 71 in the plurality of flash tanks 8a to 8d, which is located between the discharge water line 71 and the water supply. The connection position P2 of the line 77 is higher than the pressure of the flash tank 8b on the upstream side. In addition, the temperature of the water flowing in the water supply line 77 is higher than the saturation temperature, and this saturation temperature corresponds to the temperature of the water in the discharge water line 71 in the plurality of flash tanks 8a to 8d. The flow direction is at the pressure of the flash tank 8c on the downstream side of the connection position P1 of the discharge water line 71 and the feed water line 77 .

In this way, if the temperature of the water in the water supply line 75 is defined as Tw1, the temperature of the water in the water supply line 75 is defined as Tw2, the saturation temperature of the vapor corresponding to the pressure Pa of the vapor in the flash tank 8a is defined as Ta, and the temperature of the water in the flash tank 8a is defined as Ta, The saturation temperature of the vapor corresponding to the pressure Pb of the vapor in the tank 8b is defined as Tb, the saturation temperature of the vapor corresponding to the pressure Pc of the vapor in the flash tank 8c is defined as Tc, and the pressure Pd of the vapor in the flash tank 8d The saturation temperature of the corresponding vapor is defined as Td, which satisfies Ta>Tw1>Tb>Tw2>Tc>Td.

According to the configuration shown in FIG. 8, a plurality of flash tanks 8a to 8d with different pressures are provided, and the feed water of the plurality of places is fed into the place of the appropriate temperature of the discharge water line according to the temperature, so that the heat utilization efficiency can be improved. In addition, by sequentially sending the saturated water in the flash tanks 8a to 8d to the flash tank 8 with low pressure and temperature for flash evaporation, heat can be recovered according to the temperature, and the heat utilization efficiency can be improved.

In some embodiments, for example, as shown in FIG. 9 , the steam generator 6 ( 6B) is configured to use a part of the water discharged from the outlet of at least one carbon economizer among the plurality of carbon economizers 22 and 24 as a heat source. use. In the system shown in FIG. 9 , a part of the water discharged from the outlets of the plurality of carbon economizers 22 and 24 is supplied as a heat source to the heat exchangers 120 and 122 provided outside the exhaust heat recovery boiler 5 .

The water supply line K branched from the water supply line 53 is connected to the heat exchanger 120 provided on the suction line connected to the inlet of the compressor 12, and a part of the heated water comes out from the outlet of the first low-pressure carbon economizer 22 , The system is supplied to the heat exchanger 120 through the water supply line K, and the intake air of the compressor 12 is heated by heat exchange in the heat exchanger 120 . The heated water supplied to the heat exchanger 120 through the feed water line K is returned to the condenser 108 through the feed water line L after passing through the heat exchanger 120 . The heat exchanger 120 in this case is a type of heat utilization equipment. By heating the intake air of the compressor 12, the effect of preventing condensation and freezing of moisture in the intake air can be obtained when the air temperature is low or when the angle of the inlet guide vane (IGV) is reduced, and the effect of preventing the condensation of water in the intake air, and reducing the power requirement. The effect of the time zone being able to operate at low output. Even when the temperature of the intake air is high, it is about 40°C. Generally, if the inlet feed water of the low-pressure evaporator 26 (the first evaporator) of 140°C to 180°C is used for heating, the heat of a higher temperature than necessary will be used. , the heat utilization efficiency is low. By using the heating water from the outlet of the first low-pressure carbon economizer 22 with the inlet feed water of the lower-pressure evaporator 26 (the first evaporator) to be low-temperature for the heating of the intake air, the heat of the low-temperature can be effectively utilized to heat the intake air. Gas heating can improve heat utilization efficiency. Heat at a temperature of more than 100°C can generate water vapor at normal pressure, and heat at a temperature of more than 100°C has a very different utilization value than heat below 100°C. Therefore, if the inlet water of the low pressure evaporator 26 (first evaporator) at 140°C to 180°C is used to heat the heating medium with heat below 100°C, which has low utility value, the utility value of heat will be greatly lost. Conversely, if the heated water at the outlet of the first low-pressure carbon economizer 22 whose inlet feed water temperature is low to the lower-pressure evaporator 26 (the first evaporator) is used to heat the heated medium below 100°C, no significant damage will occur. The utilization value of heat can improve the heat utilization efficiency.

The water supply line M branched from the water supply line 63 is connected to a heat exchanger provided in a fuel supply line for supplying fuel to the burner 14 122, a part of the heated water from the outlet of the second low-pressure carbon economizer 24 is supplied to the heat exchanger 122 through the water supply line M, where the fuel supplied to the burner 14 is converted by heat exchange in the heat exchanger 122. preheat. The heated water supplied to the heat exchanger 122 through the water supply line M flows through the water supply line N into the condensed water line 51 after passing through the heat exchanger 122 . As described above, with regard to the heat exchangers 120 and 122, the heat utilization efficiency can be improved by appropriately selecting and utilizing the heated water at the carbon economizer outlet having a temperature close to the required temperature, respectively.

In some embodiments, for example, as shown in FIG. 9 , the steam generator 6 ( 6B) is configured to supply water to the inlet of at least one carbon economizer among the plurality of carbon economizers 22 and 24 . A part of the flowing water is used as a cooling medium, and the exhaust heat is recovered. In the method shown in FIG. 9 , part of the water flowing in the pipes 48 and 53 connected to the inlet of the carbon economizer 22 is connected to the heat exchangers 124 , 126 , 128 , 129, 130, and 132 are supplied as cooling media.

The water supply line A branched from the water supply line 70 is connected to the heat exchanger 124 . The heat exchanger 124 is provided in the cooling air line 134 that supplies part of the air compressed by the compressor 12 to the burner 14 as cooling air, and part of the water from the second low-pressure carbon economizer 24 passes through the feed water. The line A is supplied to the heat exchanger 124, and the cooling air is cooled by the heat exchange in the heat exchanger 124. The heated water supplied to the heat exchanger 124 through the feed water line A flows through the feed water line B into the feed water line 76 after passing through the heat exchanger 124 .

The water supply line C branched from the water supply line 48 is connected to the cooling medium cooler 126 for cooling the cooling medium of the generator 19 . A part of the water flowing in the water supply line 48 is supplied to the cooling medium cooler 126 through the water supply line C, and the cooling medium is cooled in the cooling medium cooler 126 by heat exchange. The water supplied to the cooling medium cooler 126 through the water supply line C is supplied to the lubricating oil cooler 128 for cooling the lubricating oil used in the bearing 127 of the compressor 12, and the lubricating oil is cooled by heat exchange. The water supplied to the cooling medium cooler 126 passes through the cooling medium cooler, returns to the water supply line 48 through the water supply line D, and flows into the first low-pressure carbon economizer 22 .

The water supply line E branched from the water supply line 48 is connected to the heat exchanger 129 . The heat exchanger 129 is provided in the suction line 138 that supplies the air extracted from the compressor 12 to the turbine 16, and a part of the water flowing in the water supply line 48 is supplied to the heat exchanger 129 through the water supply line E, and is heated in the heat exchanger 129. The exchanger 129 cools the air extracted from the compressor 12 by heat exchange. The water supplied to the heat exchanger 129 from the feed water line E flows into the feed water line 52 through the feed water line F.

The water supply line G branched from the water supply line 48 is connected to the heat exchanger 130 . The heat exchanger 130 is installed on the downstream side of the heat exchanger 124 in the cooling air line 134, and a part of the water flowing in the water supply line 48 is supplied to the heat exchanger 130 through the water supply line G, and the heat exchanger 130 The cooling air is cooled by heat exchange. The heated water supplied to the heat exchanger 130 through the feed water line G flows through the feed water line H into the feed water line 52 after passing through the heat exchanger 130 . Further, on the downstream side of the heat exchanger 130 in the cooling air line 134, a compressor 140 for compressing cooling air is provided.

The water supply pipeline I branched from the water supply pipeline 53 is connected to Heat exchanger 132 . The heat exchanger 132 is provided in the suction line 136 that supplies the air sucked from the downstream side of the position where the compressor 12 is connected to the suction line 138 to the suction line 136 of the turbine 16, and a part of the water flowing in the water supply line 53 , is supplied to the heat exchanger 132 through the water supply line I, and the air drawn from the compressor is cooled in the heat exchanger 132 by heat exchange. The water supplied to the heat exchanger 132 from the feed water line I flows through the feed water line J into the feed water line 54.

In this way, by utilizing a part of the water discharged from the outlet of at least one carbon economizer among the plurality of economizers 22 and 24 as a heat source, the heat utilization efficiency of the composite plant 2 as a whole can be improved.

In addition, by using a part of the water flowing in the pipeline for supplying water to the inlet of at least one of the plurality of carbon economizers 22 and 24 as a cooling medium to recover exhaust heat, the overall efficiency of the complex plant 2 can be improved. heat utilization efficiency.

Further, as shown in FIG. 9 , when the utilization of low-temperature exhaust heat or the recovery of low-temperature exhaust heat is performed at various temperatures, the water supply flow rates of the water supply line 48 and the water supply lines 52, 53, and 63 vary depending on the temperature level, resulting in the first The flow rate of the feed water flowing in the low pressure economizer 22 and the second low pressure economizer 24 changes, and the slope of the TQ diagram (see, for example, FIG. 5 ) is not ideal from the viewpoint of size reduction of the low pressure economizer. Here, the amount of water used for flash evaporation is adjusted for each temperature level, for example, using the pressure reducing valve 59, and by adjusting the flow rates of the feed water flowing in the first low-pressure carbon economizer 22 and the second low-pressure economizer 24, the 1. The slope of the TQ diagram of the feed water flowing in the low-pressure economizer 22 becomes close to the inclination of the TQ diagram of the exhaust gas, and the temperature of the feed water outlet of the second low-pressure economizer 24 is adjusted. When the temperature is close to the saturation temperature at the operating pressure of the low-pressure evaporator 26 (first evaporator) (the approach temperature difference is made close to 0), the carbon economizers 22 and 24 of small size can be obtained with high efficiency.

In some embodiments, the configuration in which the feed water in the compound plant 2 (2B) described in FIG. 9 is used as a heat source or a cooling medium, as shown in FIG. 10 , can also be applied to the above-described configuration with a plurality of flash tanks 8a to 8d. Compound Plant 2 (2D) of (multi-stage flash). As shown in Fig. 10, if the structure of multi-stage flash evaporation is adopted, and the feed water is recovered to a place close to the saturation temperature for flash evaporation, higher efficiency can be obtained. In this case, the feed water used as a heat source or a cooling medium is between the feed water line 21 connecting the condenser 108 and the low-temperature heat exchanger 23 and each heat exchanger 20, that is, the feed water of the low-temperature heat exchanger 23 One of the outlet, the feed water outlet of the first low pressure economizer 22, the feed water outlet of the second low pressure economizer 24, the feed water outlet of the third low pressure economizer 25 (the feed water inlet of the low pressure evaporator 26 (first evaporator)) Among the above-mentioned places, if the feed water obtained from the place with the desired temperature and after use is recovered to the place with the closest temperature, the heat utilization efficiency can be improved, which is satisfactory.

The TQ line diagram corresponding to FIG. 10 is shown in FIG. 13 . In this figure, the water supply system is supplied from the right side, and passes through the low-temperature heat exchanger (23 in Figure 10), the first low-pressure carbon saver (22 in Figure 10, the third carbon saver), and the second low-pressure zone. The carbon collector (24 in Figure 10, the first carbon collector) and the third low-pressure carbon collector (25 in Figure 10, the second carbon collector) are heated, and the feed water is passed through the third low pressure carbon collector. (25 in Fig. 10, second carbon collector) A water supply line 54 (sixth water supply) constituted so as to be supplied to the low-pressure evaporator 26 (first evaporator) without heat exchange with the heat medium (exhaust gas). line), which is fed to the low pressure evaporator (Figure 10 26, 1st evaporator). The low temperature heat exchanger (23 in Fig. 10) is supplied with feed water. The feed water acquisition line E is to use a part of the feed water from the low-temperature heat exchanger (23 in FIG. 10 ) as feed water to be the cooling and heat source of the cooling air cooler 129, which is a heat utilization device for cooling the cooling medium, that is, the cooling air. and get it. In addition, the feed water from the low-temperature heat exchanger (23 in Fig. 10) and supplied to the first low-pressure carbon economizer (22 in Fig. 10, the third economizer) is mixed with the flash tank 8d. The condensed water is mixed through the condensed water line (feed water supply line) 51 and the feed water pump 61 .

In this embodiment, the temperature of the condensed water at the outlet of the lower temperature heat exchanger (23 in FIG. 10 ) is higher, so on the TQ diagram ( FIG. 13 ), the lower temperature heat exchanger ( FIG. 10 ) 23) in the outlet feed water, the temperature of the feed water at the inlet of the first low-pressure carbon economizer (22 in Figure 10, the third carbon economizer) is high. Further, in the low-temperature heat exchanger (23 in FIG. 10 ), part of the moisture in the exhaust gas condenses in the middle to release latent heat, so the slope of the TQ diagram of the exhaust gas on the downstream side of the exhaust gas becomes small. . In addition, condensed water will be added to the first low-pressure carbon economizer (22 in Figure 10, the third carbon economizer), so the flow rate of the feed water to the lower temperature heat exchanger (23 in Figure 10) is large, and the first low-pressure zone The slope of the TQ plot of the feed water to the carbonizer (22 in Fig. 10, section 3 carbonizer) is smaller than that of the low temperature heat exchanger (23 in Fig. 10).

A part of the feed water at the outlet of the first low-pressure carbon economizer (22 in FIG. 10, the third economizer) is obtained from the feed water pipeline K as a heat utilization device for heating the suction of the compressor 12 of the gas turbine 4, namely The feed water of the heat source of the heat exchanger 120 is obtained, and the feed water acquisition line G is used to cool the cooling air that becomes the cooling air for cooling the combustor of the gas turbine 4 The cold and heat source of the device 130 is obtained, and the feed water of the heat exhaust is recovered. In addition, a part of the feed water at the outlet of the first low-pressure carbon economizer (22 in FIG. 10, the third economizer) is sent to the flash tank 8c through the feed water line (feed water acquisition line) 77 . Due to the acquisition of this water, the flow rate of the feed water flowing in the second low pressure economizer (24 in Fig. 10, the first economizer) is higher than that in the first low pressure economizer (22 in Fig. 10, the 3rd economizer). Carbonizer) is less, and the slope of the TQ diagram of the feed water of the second low-pressure carbon saver (24 in Figure 10, the first carbon saver) is higher than that of the first low-pressure carbon saver (22 in Figure 10, the 3rd step). carbon device) is large.

The outlet of the second low-pressure carbon economizer (24 in Fig. 10, the first carbon economizer), that is, the feed water at the inlet of the third low-pressure economizer (25 in Fig. 10, the second economizer), is heated by heat The utilization equipment, namely, the cooling air coolers 129 and 130, is used as a cold and heat source to absorb and exhaust the water, which is mixed by the water supply pipelines F and H, and the pipeline I is obtained from the supply water, which is used as the heat utilization equipment, that is, the cooling air cooler. The cold and heat source of 132 is obtained, and is supplied as a heat source to the fuel preheater 122 , which is a heat utilization device, through the feed water obtaining line M. In this example, the feed water temperature at the inlet of the third low-pressure carbon economizer (25 in Figure 10, the second carbon economizer) is higher than that of the second low-pressure economizer (24 in Figure 10) The temperature of the feed water at the outlet of the 1st carbonizer) is slightly lower (Figure 13). Here, compared with the cooling air coolers 129 and 130, the cooling air cooler 132, which is the cooling medium, has a higher temperature. Therefore, the cooling air cooler 132 having a higher temperature of the cooling medium is supplied with a higher temperature than the cooling air cooler 132. The cooling air coolers 129 and 130 where the temperature of the medium is low are high temperature feed water as the cooling and heat source. Thereby, the exhaust heat of the cooling air cooler, that is, the heat utilization equipment, can be recovered to a cooling medium with a temperature closer to the temperature, and can be effectively utilized, Heat utilization efficiency is improved.

As above, for the exit of the 2nd low pressure carbon economizer (24 in Fig. 10, the 1st economizer), that is, the inlet of the 3rd low pressure economizer (25 in Fig. 10, the 2nd economizer) For water supply, there are various water supply pipelines and water supply pipelines, and various types of water supply are given and received. In this embodiment, the structure is from the outlet of the second low-pressure carbon economizer (24 in FIG. 10, the first carbon economizer), that is, the third low-pressure economizer (25 in FIG. 10, the second economizer) The amount of feed water obtained from the inlet of the device) is more than the amount of feed water supplied. Therefore, the mass flow rate of the feed water flowing to the 3rd low pressure economizer (25 in Fig. 10, 2nd economizer) is higher than that of the feed water flowing into the 2nd low pressure economizer (24 in Fig. 10, 1st segment). The mass flow rate of the feed water in the carbon collector) is less, and the slope of the TQ diagram of the third low-pressure carbon collector (25 in Figure 10, the second carbon collector) is lower than that of the second low-pressure 24, Section 1 carbon device), the slope of the TQ line graph is large (Fig. 13). By realizing such a slope of the TQ graph, in the second low-pressure carbon economizer (24 in Fig. 10, the first carbon economizer), the slope of the TQ graph of the feed water becomes close to the TQ graph of the exhaust gas. The slope of the exhaust gas-feed water temperature difference can be kept close to a certain moderate temperature difference.

In addition, the flow rate of the third low-pressure carbon saver (25 in Fig. 10, the second carbon saver) is small, and the slope of the TQ diagram is large, so that the third low pressure carbon saver (25 in Fig. 10, the 2nd step) The carbonizer) can supply the low-pressure evaporator 26 (first evaporator) with water at a temperature close to the saturation temperature (in FIG. 13 , the horizontal line) corresponding to the vapor pressure of the low-pressure evaporator 26 (first evaporator), while In view of the flow of the heat medium, the heat exchanger (carbon economizer) disposed on the downstream side can sufficiently ensure the temperature difference between the exhaust gas (heat medium) and the feed water. Therefore, the heat of small size can be The exchanger (carbon economizer) achieves higher heat utilization efficiency.

Furthermore, the mass flow rate of the feed water flowing to the third low-pressure carbon economizer (25 in Fig. 10, the second carbon economizer) is higher than that of the feed water flowing to the first low-pressure economizer (22 in Fig. 10, the 3rd economizer). The mass flow rate of the feed water in the carbon collector) is less, the slope of the TQ line graph of the feed water of the third low-pressure carbon saver (25 in Figure 10, the second carbon saver) is lower than that of the first low-pressure carbon saver (Figure 10). The slope of the TQ line graph of the feed water in 22, Section 3 carbon device) is large, which is more satisfactory. With this configuration, the temperature difference between the exhaust gas and the feed water can be kept at an appropriate temperature difference close to a certain temperature from the heat medium (exhaust gas) to the downstream side, and a small-sized heat exchanger ( carbon economizer) to obtain high heat utilization efficiency. Also, the flow rate of the feed water of the third low-pressure economizer (25 in FIG. 10, the second economizer) is compared with all economizers (heat exchangers) on the downstream side when viewed from the heat medium (exhaust gas). Less is better. In this case, a heat exchanger (carbon economizer) with a smaller size can obtain high heat utilization efficiency.

In addition, as described above, in the flow direction of the heat medium in the heat medium (exhaust gas) flow path, the lower pressure evaporator (26, the first evaporator) is on the downstream side, including the second low pressure carbon economizer. (24 in Figure 10, the first carbon saver) and the third low pressure carbon saver (25 in Figure 10, the second carbon saver), and obtained from a plurality of carbon savers The water supply pipeline for a part of the water from the outlet of one carbon economizer, or the water supply pipeline for supplying feed water to the inlet of one carbon economizer in a plurality of carbon economizers, if there is at least one, Then, by obtaining or supplying feed water to adjust the feed water flow rate of the carbon economizer before and after, the slope of the TQ diagram as above can be achieved, and the heat exchanger (carbon economizer) with small size can achieve higher heat utilization efficiency. . In particular, there are at least one of the two or more water supply pipelines for obtaining a part of the water from the outlet of the different carbon economizers, and the two or more water supply lines for supplying the feed water to the inlets of the different carbon economizers, respectively, Then, the feed water can be obtained from a place with a moderate temperature suitable for the utilization of the heat utilization equipment of the feed water, or the feed water can be supplied to a place close to the temperature, which can improve the heat utilization efficiency and the plant efficiency. In addition, if both the water supply line and the water supply line are provided, the heat utilization efficiency can be more effectively improved, and the plant efficiency can be improved.

In addition, it is preferable to supply the feed water to the feed water supply line whose temperature is lower than that of the feed water outlet of the carbon economizer to which feed water is supplied to the feed water inlet, and which is higher than the temperature of the feed water outlet in the flow direction of the heat medium (exhaust gas). The carbon economizer for supplying the feed water to the feed water inlet is set to the feed water where the feed water inlet temperature of the carbon economizer is further downstream. By setting it as such a structure, the temperature difference of the feed water of a mixing place and the feed water to be supplied can be reduced. Therefore, it is possible to reduce the feed water inlet temperature of the carbon economizer for supplying feed water to its inlet, and to connect the feed water line to the downstream side (upstream side in the feed water flow direction) in the flow direction of the heat medium (exhaust gas). The temperature difference between the temperature of the feed water outlet of the carbonizer. For example, in the embodiments of FIGS. 10 and 13 , the temperature of the feed water supplied by the feed water supply lines F and H is higher than that of the feed water outlet of the third low-pressure carbon saver (25 in FIG. 10 , the second carbon saver). The temperature of the feedwater is lower than that of the feedwater inlet temperature of the second low pressure carbon economizer (24 in Figure 10, the first carbon economizer), so the temperature of the feedwater supplied by the feedwater supply lines F and H is close to that of the third low pressure The temperature of the feed water flowing between the carbon economizer (25 in Figure 10, the 2nd carbon economizer) and the second low pressure economizer (24 in Figure 10, the 1st economizer) can reduce the temperature of the 2nd low pressure economizer Carbon device (Figure 10 The temperature difference between the feed water outlet of 24 in the 1st carbon segment and the feed water inlet of the 3rd low pressure carbon segment (25 in Figure 10, the 2nd carbon segment).

Therefore, in the TQ diagram (Fig. 13), the left end of the water supply line (equivalent to the water supply outlet) corresponding to the second low-pressure carbon saver (24 in Fig. 10, the first carbon saver) and the 3 The temperature difference between the right end (equivalent to the feed water inlet) of the feed water line of the low-pressure carbon economizer (25 in Figure 10, the second carbon economizer) can make the second low-pressure economizer (24 in Figure 10, part 2). The temperature difference between the heat medium (exhaust gas) and the feed water between the feed water outlet of the 1 carbon economizer and the feed water inlet of the 3rd low pressure economizer (25 in Figure 10, the 2 carbon economizer) is set to a close value, which can be Small size heat exchanger (carbon economizer) to obtain high heat utilization efficiency.

Furthermore, a part of the feed water at the outlet of the second low-pressure carbon economizer (24 in Fig. 10, the first carbon economizer) is sent to the flash tank 8b via the feed water line 73, and the steam generated by the reduced pressure boiling is supplied to the flash tank 8b. To the middle section of the low pressure steam turbine, its power is taken out. Furthermore, a part of the feed water at the outlet of the second low-pressure carbon saver (24 in Figure 10, the first carbon saver) is sent to the low-boiling-point medium blue-gold cycle 142, where it will flow inside the low-boiling-point medium blue-gold cycle 142. The circulating low boiling media (eg, pentane, cyclohexane, R245fa, etc.) is heated. The heated, low-boiling medium evaporates and drives a turbine to generate power. As described above, the combination of the flash tanks 8a to 8d and the low-pressure steam turbine 106, and the low-boiling-point medium blue-gold cycle 142 are provided in the heat medium flow path in which the exhaust gas (heat medium) flows, and the heating feed water will be obtained. In the feed water acquisition pipeline of the feed water between the plurality of heat exchangers (carbon economizers), the feed water obtained from at least one of them is sent to the power generation device, and the power generation device uses the received feed water to generate power.

According to this configuration, the heat of the water supply can be effectively utilized to extract power, and the efficiency of the plant can be improved. In addition, the flow rates of the feed water lines (feed water acquisition lines) 73, 75, and 77 are adjusted by the pressure reducing valve 84 and the flow rate adjustment valves 205 and 206, respectively, so that the feed water outlet temperature of the third low-pressure carbon economizer 25 is close to the low-pressure evaporator 26. (1st evaporator) saturation temperature at the operating pressure (to make the approach temperature difference close to 0), and to adjust the flow rates of the second low pressure carbon economizer 24 and the third low pressure economizer 25 so that the second low pressure economizer 24 The slopes of the TQ diagrams of the feed water of the third low-pressure carbon economizer 25 are respectively close to the slopes of the TQ diagrams of the exhaust gas. If the flow rate of the water supply lines (water supply pipelines) 73, 75, and 77 is increased, the self-supplied water at the respective branch points is regarded as the upstream carbon economizer, that is, the third low-pressure economizer 25 and the second low-pressure economizer. As the feed water flow rate of the device 24 and the first low-pressure carbon economizer 22 increases, the slope of the TQ diagram decreases.

Conversely, in order to increase the slope of the respective TQ diagrams, the flow rates of the water supply lines 73, 75, and 77 may be decreased. In this way, the temperature of the feed water outlet of the third low pressure economizer 25 (the feed water inlet of the low pressure evaporator 26) can be made close to the saturation temperature corresponding to the operating pressure of the low pressure evaporator 26, and the first low pressure economizer 22 . The slope of the TQ diagram of the feed water of the second low-pressure carbon economizer 24 is close to the inclination of the TQ diagram of the exhaust gas, so that the heat utilization efficiency can be improved with a smaller size economizer. In addition, the structure of the low-boiling-point medium sapphire cycle 142 in the present embodiment is merely an example, and various low-boiling-point medium sapphire cycles of various configurations can be appropriately employed. Various structures are disclosed in Japanese Patent Application Laid-Open No. 2015-183595, so if reference is made, it is understood that various structures can be applied by those in the field.

Intake of gas turbine 4 without power generating means In the heat utilization equipment in the factory such as the heater 120, the cooling air coolers 129, 130, 132, the fuel preheater 122, etc., the flow rate of the water supply that becomes the necessary heat source and the cold and heat source is determined according to the necessity of heating or cooling. , cannot be set freely. On the other hand, the power generator can appropriately give the temperature and flow rate of the feed water to be the heat source, and generate power according to the temperature and flow rate of the obtained feed water. Therefore, if a power generation device is provided as in the present embodiment, even when it is necessary to supply feed water of the necessary temperature and flow rate to the heat utilization equipment in various factories, by changing the water supply to the power generation device The flow rate or the acquisition position between the carbon economizers, as mentioned above, can improve the flow distribution of the feed water flowing in the plurality of carbon economizers, so that the feed water temperature at the inlet of the low pressure evaporator (the first evaporator 26) is close to that of the low pressure evaporator. The vapor pressure of the (first evaporator 26) corresponds to the saturation temperature, and the temperature difference between the heat medium (exhaust gas) and the feed water of each part can be kept at a moderate temperature, and a small-sized heat exchanger (carbon economizer) can be maintained. ) to obtain high heat utilization efficiency.

Furthermore, in some embodiments, as shown in FIG. 1 , the whole amount of water heated by the second carbon collector 24 is sent to the low-pressure evaporator 26 (first evaporator), or heated to a relatively low-pressure evaporator 26 The saturation temperature of the vapor pressure of (1st evaporator) is at least one of high temperature heat exchangers of high temperature. In FIG. 1, the whole amount of water heated by the second carbon economizer 24 is sent to any one of the low pressure evaporator 26 (the first evaporator), the medium pressure economizer 31, and the first high pressure economizer 30, Do not supply to other heat utilization equipment. The intermediate-pressure carbon economizer 31 and the first high-pressure economizer 30 are pressurized to feed water by the intermediate-pressure feed pump 62 and the high-pressure feed pump 72, respectively. In the medium-pressure economizer 31 and the first high-pressure economizer 30, since the feed water is boosted, the corresponding low-pressure evaporator 26 (first evaporator) It will not boil at the saturation temperature of the vapor pressure, but is in the liquid phase, and can be heated to higher temperatures. The feed water heated by the medium pressure economizer 31 and the first high pressure economizer 30 is evaporated by the medium pressure evaporator 32 and the high pressure evaporator 38 respectively, and finally drives the steam turbine to generate power.

The feed water heated by the second carbonizer 24 that directly sends the feed water to the low-pressure evaporator 26 (the first evaporator) will not be sent to various heat utilization equipment for low-temperature heat utilization, but limited to the low-pressure evaporator. The evaporator 26 (the first evaporator), the intermediate pressure carbon economizer 31 and the first high pressure economizer 30 are heated to a higher temperature than the saturation temperature corresponding to the vapor pressure of the low pressure evaporator 26 (the first evaporator), thereby , the flow rate of the feed water heated by the second carbon device 24 can be reduced. Accordingly, the temperature distribution of the feed water flowing in the carbon economizer can be made close to the above-mentioned preferable temperature distribution, and the slope of the line corresponding to the feed water of the second carbon economizer 24 on the TQ diagram can be made larger, so that the supply to the low pressure can be made larger. The temperature of the feed water of the evaporator 26 (the first evaporator) is close to the saturation temperature corresponding to the vapor pressure of the low pressure evaporator 26 (the first evaporator), so that the heat utilization efficiency can be improved. In this case, for various heat utilization equipments for utilization of low-temperature heat, relatively low-temperature feed water is obtained from between the carbon economizers and sent out (water supply line 53).

Furthermore, in some embodiments, as shown in FIG. 10 , part of the air at the outlet of the compressor 12 of the gas turbine 4 is obtained as cooling air for cooling the combustor of the gas turbine 4 . This cooling air can reduce the power to send the cooling air to the compressor 140 of the combustor, and in order to improve the cooling effect when the combustor is cooled, the heat exchanger 130 is used to cool and reduce the temperature. On the other hand, a part of the feed water at the outlet of the first low-pressure economizer 22 is supplied to the heat exchanger 130 as a cooling medium. Heat Exchanger 130 In the process, the cooling air is cooled and the feed water is heated by exchanging heat between the cooling air and the feed water. That is, the heat exchanger 130 is a heat utilization device that utilizes the feed water as a cold and heat source. In addition, cooling air is a kind of medium to be cooled.

The temperatures of the cooling air at the inlet and outlet of the heat exchanger 130 are, for example, 180°C and 90°C, respectively, and the temperatures of the feed water at the inlet and outlet of the heat exchanger 130 are 80°C and 130°C, respectively. Here, the heat at a temperature exceeding 100°C can generate steam at normal pressure, and the heat at a temperature exceeding 100°C and the heat at a temperature below 100°C are significantly different in utilization value. Therefore, as in this example, the exhaust heat from the cooling air temperature reduction is effectively utilized, and if the water at the outlet of the carbon economizer, which does not reach 100°C, is heated to a temperature higher than 100°C, the valuable heat can be recovered and utilized. , especially to improve heat utilization efficiency.

In this case, since a sufficient cooling effect can be obtained in the burner, the heat exchanger 130 needs to cool the cooling air, which is the medium to be cooled, to the lower-pressure evaporator 26 (the first evaporator). ), the saturation temperature (eg, 150° C.) at the vapor pressure is a low temperature. At this time, assuming that the heat exchanger 20 is a single unit, the water that will be the inlet or the outlet of the single heat exchanger 20 is used for cooling the to-be-cooled medium. In the single heat exchanger 20, the temperature of the feed water outlet has become a temperature close to the saturation temperature under the vapor pressure of the low-pressure evaporator 26 (the first evaporator), so that the cooling medium cannot be cooled to a sufficiently low temperature, and The feed water at the inlet of the heat exchanger 20 will be used for cooling. Therefore, it becomes the feed water that recovers the exhaust heat when the cooling medium is cooled to a low temperature, and the exhaust heat cannot be effectively recovered, and the heat utilization efficiency is low.

Therefore, as in the present invention, if a plurality of heat exchangers 20 are provided, and feed water is obtained therefrom and used for heat recovery, even if it is necessary to cool the cooling medium to the lower-pressure evaporator 26 (first evaporator) When the saturation temperature (for example, 150° C.) under the vapor pressure is low, the exhaust heat can still be recovered in the feed water of moderate temperature, and the exhaust heat can be recovered efficiently.

In some embodiments, for example, as shown in FIG. 11 , the number of low-pressure carbon economizers may also be one. In the compound plant 2 ( 2E ) shown in FIG. 11 , instead of the first low pressure economizer 22 and the second low pressure economizer 24 of the compound plant 2 ( 2C) shown in FIG. 7 , one low pressure economizer 96 is provided .

In the configuration shown in FIG. 11 , the feed water line 48 connects the condenser 108 to the low pressure economizer 96 . The low pressure economizer 96 heats the water supplied from the water line 48 by heat exchange with the exhaust gas. A portion of the water heated by the low pressure economizer 96 is supplied to the low pressure evaporator 26 through the feed water line 52 connecting the low pressure economizer 96 and the low pressure evaporator 26 .

In addition, a part of the water heated by the low-pressure carbon economizer 96 is supplied to the medium-pressure economizer 31 via the water supply line 60 . The water supply line 60 is branched from the water supply line 54 and connected to the medium pressure carbon saver 31. The heating water flowing in the water supply line 60 is sent to the medium pressure carbon saver by the medium pressure water pump 62 set on the water supply line 60. device 31.

The flash tank 8 is connected with a water supply line 53 branched from the water supply line 52 , and a part of the water heated by the low-pressure carbon economizer 96 is supplied to the flash tank 8 through the water supply line 53 . The water supply line 53 is provided with a pressure reducing valve 59 for reducing the pressure of the heating water supplied from the low pressure carbon economizer 96 . The heated water supplied to the flash tank 8 via the water supply line 53 is evaporated under reduced pressure from the flash tank 8 (flash tank 8). steam), which becomes flash vapor. The flash steam produced by the flash tank 8 is supplied to the middle section of the low pressure steam turbine 106 via a steam line 57 connecting the flash tank 8 and the middle section of the low pressure steam turbine 106 .

The condensed water accumulated at the bottom of the flash tank 8 flows into the water supply line 48 through the condensed water line 51 connecting the flash tank 8 and the water supply line 48 , and is supplied to the low pressure carbon economizer 96 via the water supply line 48 . The condensate water pipeline 51 is provided with a feed water pump 61 , and the condensate water discharged from the flash tank 8 is sent to the low pressure carbon economizer 96 by the feed water pump 61 .

In this case, even if the feed water is obtained from one location and the flash steam generated by flash evaporation is used in the case of overheating the feed water before the flash evaporation, the steam with a higher temperature can be used than in the case of not superheated, which can improve the heat utilization. efficiency. In addition, by making the steam into a superheated state, condensation in the piping such as the steam line 57 can be suppressed, and troubles such as clogging of the piping due to drain water can be suppressed. In addition, when the steam from the superheater 69 is used in a steam turbine, the wetting of the downstream section of the steam turbine can be reduced, the corrosion of the turbine airfoil can be suppressed, and the efficiency of the steam turbine can be improved.

In some embodiments, for example, as shown in FIG. 12 , the composite plant 2 ( 2F ) may be configured as a steam-electricity cogeneration plant using the steam generated by the steam generator 6 as a heat source.

In the compound plant 2 (2F) shown in FIG. 12, the steam generated from the steam generator 6, that is, the steam flowing in the steam lines 58, 92, 93, 94, 95, and 117, can be used for chemical reactions, food processing, etc. , Air conditioning (heating room with steam as heat source or cold room used as heat source of absorbing refrigerator, etc.) etc. In the exemplary embodiment shown in FIG. 12, the exhaust heat recovery pot A heat exchanger 116 is provided outside the furnace 5, and the high-pressure superheated steam superheated by the second high-pressure superheater 44 is supplied to the heat exchanger 116 through a steam line 117 connecting the second high-pressure superheater 44 and the heat exchanger 116. In the heat exchanger 116, the high-pressure superheated steam supplied via the steam line 117 can also be used for the above-mentioned purposes. The high-pressure superheated steam subjected to the superheat exchange by the heat exchanger 116 is supplied to the first reheater 42 through the steam line 118 provided with the valve 119 .

In the compound plant shown in FIG. 10, the water supply lines 73, 75, and 77 for supplying water to the flash tanks 8a, 8b, and 8c are provided with a pressure reducing valve 84 and flow rate adjustment valves 205, 206, respectively. By adjusting the opening degree of each of these valves, the flow rate of the feed water supplied to the flash tanks 8a, 8b, and 8c can be adjusted. According to this configuration, since the flow rate of each heat exchanger 20 (carbon economizer) can be adjusted, high heat utilization efficiency can be maintained, and the size of the heat exchanger can be reduced. The configuration for adjusting the flow rate of the feed water to be supplied to the above flash tank is illustrated and described using the composite plant in FIG. 10 as an example, but it can be applied to other embodiments.

Moreover, in the compound plant shown in FIG. 10, the pressure reducing valve 85 is provided in the position between the flash tank 8a and the flash tank 8b in the discharge water line 71. A pressure reducing valve 86 is provided at a position between the flash tank 8b and the flash tank 8c in the discharge water line 71 . A pressure reducing valve 87 is provided at a position between the flash tank 8c and the flash tank 8d in the discharge water line 71 .

By adjusting the opening degrees of these pressure-reducing valves 85 to 87 , the flow rate of the drain water flowing in each part of the drain water line 71 is adjusted. The liquid level can be kept constant respectively. For example, when the liquid level of the flash tank 8b upstream of the pressure reducing valve 86 rises, by increasing the opening degree of the pressure reducing valve 86, the flow rate in the pressure reducing valve 86 is increased. The flow rate of the discharge water is reduced, and the liquid level of the flash tank 8b is lowered. Conversely, when the liquid level of the flash tank 8b is lowered, by reducing the opening of the pressure reducing valve 86 to reduce the flow rate of the drain water flowing in the pressure reducing valve 86, the liquid level of the flash tank 8b can be raised. , to keep the liquid level of the flash tank 8b constant.

For the flash tank 8d without a pressure reducing valve on the downstream discharge water line, the liquid level is kept constant by controlling the flow rate of the pump 61 . Although not shown in the figure, if the pump 6 is provided with a recirculation flow path for recirculating a part of the discharge water from the outlet to the inlet, and a flow rate adjustment valve is provided on the recirculation flow path, the recirculation flow rate is adjusted by the flow rate adjustment valve. The flow rate of the pump 61 can be controlled by a method such as a method of driving the pump 61 with a motor equipped with an inverter to control the number of revolutions, or the like.

With this configuration, the liquid level of the flash tank can be kept constant, the low-pressure steam turbine 106 can be prevented from sucking in liquid through the steam lines (92 to 95), the reliability of the low-pressure steam turbine 106 can be maintained, and the flash evaporation can be maintained. A sufficient amount of liquid is maintained in the tank to ensure the amount of evaporation, so that the output of the low-pressure steam turbine 106 is sufficiently increased, and the plant efficiency is improved. The above-mentioned configuration in which the liquid level of the flash tank is kept constant is illustrated and described by taking the compound plant of FIG. 10 as an example, but it can also be applied to other embodiments.

The present invention is not limited to the above-described embodiments, and includes a mode in which changes are added to the above-described embodiment, or a mode in which these modes are appropriately combined.

For example, in the above-mentioned several embodiments, although the configuration in which the exhaust gas is supplied from the gas turbine 4 to the exhaust heat recovery boiler 5 is exemplified, the supply source for supplying the exhaust gas to the exhaust heat recovery boiler 5 is not limited to the gas turbine The turbine may be, for example, another prime mover such as a gas engine, a boiler, or a fuel cell.

Moreover, the exhaust heat recovery plant 200 provided with the steam generator 6 (6A-6F) mentioned above may be implemented by retrofitting an existing exhaust heat recovery plant.

In this case, the modification method of the exhaust heat recovery plant, for example, in order to manufacture the above-mentioned generator 6 ( 6A) shown in FIG. 1. The steps of increasing the number of carbon economizers on the downstream side of the evaporator 26 to two or more; The step of connecting the heat utilization equipment of the steam tank 8 and the like with the water supply line 53 .

Thereby, compared with the case where the temperature of the feed water is close to the saturated steam temperature with one carbon economizer, the size of the carbon economizer (the total size of two or more economizers) can be suppressed from increasing in size, and flash evaporation can be used. The heat utilization facilities such as the tank 8 improve the heat utilization efficiency of the heat medium.

The content described in each of the above-mentioned embodiments can be grasped as follows, for example.

(1) A steam generator (6) according to an embodiment of the present invention includes: a heat medium flow path (18) through which a heat medium flows; and a first carbon block (22) provided in the heat medium flow path ; In the flow path of the heat medium, the second carbon section (24) is arranged on the upstream side of the first carbon section in the flow direction of the heat medium; in the flow path of the heat medium, in the flow direction of the heat medium Flow direction setting The first evaporator (26) on the upstream side of the above-mentioned second-stage carbon device; the first water supply pipeline (52) constituted by supplying the water heated by the above-mentioned first-stage carbon device to the above-mentioned second-stage carbon device , 27); and the second water supply pipeline (53, 75) formed by branching from the aforementioned first water supply pipeline to supply the water heated by the aforementioned first carbon heater to the heat utilization equipment (8, 51, 61, 120, 122, 129, 130, 132). , 77).

According to the steam generator described in the above (1), since the first water supply line for supplying water from the first carbon section to the second carbon section is provided, and the branch for supplying water to the heat utilization facility from the first water supply line is provided. The 2nd water supply line, so the flow rate of the 2nd carbonizer is less than that of the 1st carbonizer. Therefore, according to the flow rate of the feed water supplied to the heat utilization equipment, even if the flow rate of the feed water to the 1st stage carbonizer increases, the temperature of the feedwater can be efficiently approached to the saturated steam temperature with the smaller 2nd stage carbonizer. Therefore, the size of the carbon economizer (the sum of the size of the first carbon economizer and the size of the second carbon economizer) can be suppressed from increasing in size compared with the case where the temperature of the feed water is made closer to the saturated steam temperature by one economizer , and heat utilization equipment can be used to improve the heat utilization efficiency of the heat medium.

(2) In some embodiments, in the steam generator described in the above (1), the heat utilization device is a first flash tank (8) for generating flash steam.

The steam generator described in the above (2) is provided with a first water supply line for supplying water from the first carbon tank to the second carbon tank, and a branch from the first water supply line for supplying water to the first flash tank of the 2nd water supply line, the 2nd The flow rate of the carbon saver is less than that of the first carbon saver. Therefore, according to the flow rate of the feed water supplied to the flash tank, even if the flow rate of the feed water to the first-stage carbonizer increases, the temperature of the feedwater can be efficiently approached to the saturated steam temperature with the smaller second-stage carbonizer. Therefore, the size of the carbon economizer (the sum of the size of the first carbon economizer and the size of the second carbon economizer) can be suppressed from increasing in size compared with the case where the temperature of the feed water is made closer to the saturated steam temperature by one economizer , and the heat utilization equipment can be used to improve the heat utilization efficiency of the heat medium.

(3) In some embodiments, in the steam generator described in (2) above, a plurality of evaporators (26, 32, 38) including the first evaporator are provided in the heat medium flow path; The first evaporator is an evaporator located on the most downstream side in the flow direction of the heat medium flow path among the plurality of evaporators.

The temperature of the steam and condensed water obtained by flash evaporation is lower than the temperature of the original water, so compared with the evaporator, the steam generated by the flash evaporation has lower heat utilization efficiency. When another evaporator exists on the downstream side from the heat medium (exhaust gas) of the carbon economizer from which the flash water is obtained, if the flash water is obtained, the heat is supplied to the other evaporator on the downstream side. The heat of the medium (exhaust gas) is reduced, and other evaporators on the downstream side can utilize the possible heat reduction. Therefore, the amount of steam generated from the evaporator with high heat utilization efficiency decreases, while the flow rate of flash steam increases compared with the evaporator with low heat utilization efficiency, and the heat utilization efficiency decreases. On the other hand, according to the steam generator described in the above (2), feed water is obtained from the evaporator on the most downstream side in the flow direction of the heat medium flow path, that is, from the carbon economizer further downstream than the first evaporator, and preliminarily flash Therefore, the flash steam can be obtained without reducing the amount of steam generated by the evaporator, so the heat of the heat medium can be effectively utilized without reducing the heat utilization efficiency, and the effect of improving the plant efficiency is particularly large. Also, when the feed water obtained from the carbon economizer is used for purposes other than flash steam generation, if the first evaporator is located on the most downstream side in the flow direction of the heat medium flow path, it is not necessary to reduce the consumption of other evaporators. Obtaining feed water under evaporation can achieve particularly large plant efficiency improvement effects.

(4) In some embodiments, the steam generator described in the above (2) or (3) further includes: a method of supplying the water heated by the second carbonizer to the first flash tank The 3rd water supply line (63) formed; and the 4th water supply line formed so as to supply water to the above-mentioned first flash tank from branching from the water supply line for supplying water to the above-mentioned No. 1 carbon tank At least one of (E, F, G, H).

According to the steam generator described in the above (4), by supplying the feed water obtained from at least two feed water lines including the second feed water line to the first flash tank, the flow rate of the second carbon section can be adjusted, and the size of the carbon block can be adjusted appropriately. The carbon economizer obtains high efficiency. In addition, it affects the evaporation amount of the first evaporator, especially the temperature of the feed water at the outlet of the second carbon section, which is important, is kept high (the approach temperature difference of the first evaporator is kept close to 0), and the first The temperature difference between the exhaust gas and the water supply in the carbon economizer is maintained at a certain value larger than the water supply outlet of the first carbon economizer. Here, when the temperature difference between the exhaust gas and the feed water is constant, since the heat exchange amount is the largest in terms of size, it is possible to reduce the size of the first carbon device reasonably, and only the performance can be improved. especially important The efficiency of the second section of the carbon device is increased due to the larger size.

(5) In some embodiments, the steam generator according to any one of the above (2) to (4) further includes: for supplying the steam generated in the first flash tank to a utilization The first steam lines (57, 93, 94, 95) of the steam equipment (100); and a superheater ( 69,89,90,91).

According to the steam generator described in the above (5), the steam flowing in the first steam line is superheated by the superheater by using the high-temperature feed water, and the high-temperature steam can be used compared with the case where the steam is not overheated, thereby improving the heat utilization efficiency. In addition, by making the steam into a superheated state, condensation in the piping such as the steam line can be suppressed, and troubles such as clogging of the piping due to drain water can be suppressed.

(6) In some embodiments, in the steam generator according to any one of the above (2) to (5), the steam generator includes a plurality of flash tanks (8a to 8a) including the first flash tank. 8d); the pressures of the plurality of flash tanks are set to different pressures from each other.

According to the steam generator described in the above (6), by sequentially sending the saturated water in the flash tank to the flash tank with low temperature and pressure to evaporate, the heat matching temperature can be recovered and the heat utilization efficiency can be improved.

(7) In some embodiments, the steam generator described in (6) above further includes: A drain water pipeline (71) connected in series to the plurality of flash tanks for the flow of the drain water discharged from each of the flash tanks; and the water heated by the first carbon device or the second carbon device The fifth water supply line (75, 77) supplied to the above-mentioned discharge water line; the temperature of the water in the above-mentioned fifth water supply line is located in the flow direction of the above-mentioned discharge water line in the plurality of flash tanks corresponding to the above-mentioned discharge water. The pressure saturation temperature of the flash tank on the upstream side of the position where the water line is connected to the fifth water supply line is lower than that in the flow direction of the discharge water line corresponding to the plurality of flash tanks. The pressure saturation temperature of the flash tank on the downstream side of the position connected to the fifth feed water line is higher.

According to the steam generator described in the above (7), since a plurality of flash tanks with different pressures are provided, the feed water of the plurality of places can be fed into the place of the appropriate temperature of the discharge water line according to the temperature, and the heat utilization efficiency can be improved. .

(8) In some embodiments, in the steam generating device described in any one of (2) to (7) above, the steam generating device is set in the flow direction of the heat medium in the heat medium flow path The downstream side of the first evaporator includes a plurality of carbon economizers including the first carbon economizer and the second carbon economizer; at least one carbon economizer from the plurality of carbon economizers A part of the water from the outlet is used as a heat source.

According to the steam generator described in the above (8), one of the water discharged from the outlet of at least one carbon economizer among the plurality of carbon economizers is Part of it is used as a heat source, and the heat utilization efficiency can be improved considering the external structure of the steam generator.

(9) In some embodiments, in the steam generating device described in any one of (2) to (8) above, the steam generating device is set in the flow direction of the heat medium in the heat medium flow path The downstream side of the first evaporator includes a plurality of carbon economizers including the first carbon economizer and the second carbon economizer; so as to be connected with at least one carbon economizer in the plurality of carbon economizers A part of the water flowing in the water supply pipeline connected to the inlet of the device is used as a cooling medium, and the heat is recovered and exhausted.

According to the steam generator described in the above (9), the exhaust heat is recovered by utilizing a part of the water flowing in the line for supplying water to the inlet of at least one carbon economizer among the plurality of carbon economizers as a cooling medium, It is possible to improve the heat utilization efficiency considering the external structure of the steam generating device.

(10) A steam generator according to an embodiment of the present invention is provided with: a heat medium flow path (18) through which a heat medium flows; carbon economizers (96, 25) provided in the heat medium flow path; In the heat medium flow path, a first evaporator (26) arranged on the upstream side of the carbon economizer in the flow direction of the heat medium; a first flash tank (8) for generating flash steam; The first water supply lines (52, 54) through which the carbon economizer supplies water to the first evaporator are branched from the first water supply line and connected to the first water supply line of the first flash tank. 2. Water supply lines (53, 73) are provided in the second water supply lines, and superheaters (69, 88) are used to superheat the steam generated in the first flash tank by the water flowing in the second water supply lines.

(11) In some embodiments, in the steam generator described in any one of the above (2) to (10), the steam generator is configured by adjusting the valve (84, 205, 206) of the second water supply line. The opening degree was adjusted, and the flow rate of the feed water supplied to the said 1st flash tank was adjusted.

According to the steam generator described in (11) above, since the flow rate of the carbon economizer can be adjusted, high heat utilization efficiency can be maintained, and the size of the carbon economizer can be reduced.

(12) In some embodiments, in the steam generator described in any one of the above (2) to (11), the steam generator adjusts the pipeline ( 71) The opening of the valve (85, 86, 87), or at least one of the flow rate of the pump (61) provided on the pipeline for the flow of the discharge water from the first flash tank, is adjusted. The liquid level of the aforementioned first flash tank.

According to the steam generator described in the above (12), by appropriately adjusting at least one of the opening degree of the valve and the flow rate of the pump, the liquid level of the first flash tank can be adjusted to be constant.

(13) In some embodiments, in the steam generator described in the above (1), the heat utilization equipment is a connection between the medium to be heated and the first carbonizer. The heated water is exchanged for heat, or the heated medium is mixed with the water heated by the carbon device in Section 1 to heat the heated medium.

According to the steam generator described in the above (13), if the heated medium is heated by using the heating water whose temperature is lower than that of the inlet feedwater of the evaporator and the outlet of the carbonizer of the first section, the utility value of heat can be greatly reduced. to improve heat utilization efficiency.

(14) In some embodiments, in the steam generator described in the above (13), the heated medium is 100° C. or lower.

According to the steam generator described in the above (14), if the heated medium below 100°C is heated with the heating water whose temperature is lower than that of the feed water at the inlet of the evaporator, the temperature of the feed water at the outlet of the low-fat first-stage carbonizer is 100° C. Under the utilization value of heat, improve the heat utilization efficiency.

(15) In some embodiments, in the steam generator described in the above (1), the heat utilization device exchanges heat with the water heated by the cooling medium and the water heated by the first carbon device, so as to cool the cooled The media is cooled and the water heated by the carbonizer in Section 1 above is further heated.

According to the steam generator described in the above (15), even when it is necessary to cool the cooling medium to a temperature lower than the saturation temperature under the steam pressure of the first evaporator, the exhaust heat can be recovered at an appropriate temperature The feed water can be recovered efficiently.

(16) In some embodiments, in the steam generator described in (15) above, The above-mentioned heat utilization equipment heats the water heated by the above-mentioned Section 1 carbon heater to a temperature higher than 100°C.

Heat at a temperature of more than 100°C can generate water vapor at normal pressure. Heat at a temperature of more than 100°C and heat below 100°C have different utilization values. Therefore, as in the steam generator described in the above (16), the exhaust heat from the desuperheating of the cooling medium is effectively utilized to heat the water at the outlet of the carbon economizer below 100°C to a higher temperature than 100°C , the heat with high value can be recycled, especially the heat utilization efficiency can be improved.

(17) In some embodiments, in the steam generating device described in (15) or (16), the flow direction of the heat medium in the heat medium flow path of the steam generating device is more advanced than that of the first evaporator. The downstream side includes a plurality of carbon economizers including the first carbon economizer and the second carbon economizer; the plurality of carbon economizers are arranged most upstream in the flow direction of the heat medium in the heat medium flow path The carbon economizer supplies the heated feed water to the first evaporator; the heat utilization equipment cools the cooling medium to a temperature below the saturation temperature corresponding to the vapor pressure in the first evaporator.

According to the steam generator described in the above (17), even if the cooling medium is cooled to below the saturation temperature corresponding to the steam pressure of the first evaporator, the feed water is obtained from the middle of the plurality of carbon economizers and used for heat recovery. Even in the case of a suitable temperature, the exhaust heat can still be recovered in the feed water of moderate temperature, and the exhaust heat can be recovered with good efficiency.

(18) The steam generator (6) according to an embodiment of the present invention is provided with: A heat medium flow path (18) for supplying the heat medium to flow; a first carbon block (24) arranged in the heat medium flow path; The second carbon economizer (25) on the upstream side of the carbon economizer; in the heat medium flow path, the first evaporator provided on the upstream side of the second carbon economizer in the flow direction of the heat medium, the first evaporator (26); a first water supply pipeline (52, 27) formed in such a way as to supply the water heated by the aforesaid section 1 carbon container to the aforesaid section 2 carbon container; The heated water is supplied to the sixth water supply pipeline (54) formed by the method of the first evaporator without exchanging heat with the aforementioned heat medium; The water supply to the carbon device in the aforementioned section 1 is less.

According to the steam generator described in the above (18), the temperature difference between the exhaust gas and the feed water can be maintained at an appropriate temperature difference close to a certain value, and a high heat utilization efficiency can be realized with a small-sized carbon economizer.

(19) In some embodiments, in the steam generating device described in (18), the steam generating device has a flow direction of the heat medium in the heat medium flow path further downstream than the second carbon separator. , including the 3rd stage carbon device (22), the mass flow rate of the feed water flowing to the aforementioned 2nd stage charcoal device is less than the mass flow rate of the feed water flowing through the aforementioned 3rd stage charcoal device.

According to the steam generator described in the above (19), the temperature difference between the exhaust gas and the feed water can be kept in contact with the downstream side as viewed from the heat medium. Near a certain moderate temperature difference, a smaller carbon economizer can be used to obtain high heat utilization efficiency.

(20) In some embodiments, in the steam generating device described in (18) or (19), the flow direction of the heat medium in the heat medium flow path of the steam generating device is higher than that of the first evaporator The further downstream side includes a plurality of carbon savers including the first carbon saver and the second carbon saver; A portion of the feed water is taken from the lines (E, K, G, I, M, 77).

According to the steam generator described in the above (20), by obtaining the feed water to adjust the feed water flow rate of the front and rear carbon economizers, a good slope of the TQ diagram can be achieved, and a high heat utilization efficiency can be achieved with a small carbon saving. implement.

(21) In some embodiments, in the steam generator described in the above (20), the steam generator includes two or more feed waters each obtained from a part of the water discharged from the outlets of the different carbon economizers. Get the pipeline.

According to the steam generator described in the above (21), the feed water can be obtained from a place with an appropriate temperature suitable for the utilization of the heat utilization equipment using the feed water, the heat utilization efficiency can be improved, and the efficiency of the factory can be improved.

(22) In some embodiments, in the steam generating device described in (18) or (19), the steam generating device is connected to the heat in the heat medium flow path. The flow direction of the medium is further downstream than the first evaporator, and includes a plurality of carbon savers including the first carbon saver and the second carbon saver, and is provided with a carbon saver for one of the plurality of carbon savers. The inlet of the carbonizer supplies the feed water supply line with feed water.

According to the steam generator described in the above (22), by supplying feed water to adjust the feed water flow rate of the front and rear carbon economizers, the slope of the TQ diagram as well as the above can be achieved, and the carbon economizers with small size can achieve higher heat Use the carbon saver of efficiency.

(23) In some embodiments, in the steam generator described in (20) or (21), the steam generator includes feed water for supplying feed water to the inlet of one carbon economizer among the plurality of carbon economizers Supply lines (F,H).

According to the steam generator described in the above (23), including both the feed water acquisition line and the feed water supply line, the heat utilization efficiency can be more effectively improved, and the efficiency of the plant can be improved.

(24) In some embodiments, in the steam generator according to the above (22) or (23), the steam generator includes two or more feed water supplies for supplying feed water to different inlets of the carbon economizers, respectively. pipeline.

According to the steam generator described in the above (24), the feed water can be supplied to a place close to the temperature suitable for the utilization of the heat utilization equipment using the feed water, the heat utilization efficiency can be improved, and the efficiency of the factory can be improved.

(25) In several embodiments, in the steam generating apparatus described in any one of (22) to (24) above, The feed water supply line supplies feed water with a lower temperature than the feed water outlet of the carbon economizer to which the water is supplied, and the supply temperature is set further downstream than the carbon economizer to which the feed water is supplied relative to the flow direction of the heat medium. The feed water inlet of the aforementioned carbon economizer has higher feed water.

According to the steam generator described in the above (25), the temperature difference between the feed water at the mixing place and the feed water to be supplied can be reduced. Therefore, the feed water inlet temperature of the carbon economizer for supplying feed water to the inlet can be lowered, and the feed water line can be connected to the downstream side in the flow direction of the heat medium (exhaust gas) (the upstream side in the flow direction of the feed water) and installed. The temperature difference between the feed water outlet temperature of the carbon economizer. Thereby, a small-sized carbon economizer can be obtained, and high heat utilization efficiency can be obtained.

(26) In some embodiments, in the steam generating device according to any one of (20), (21) and (23) above, the steam generating device further includes a power generating device (8, 106), The feed water obtained from at least one of the feed water obtaining lines is sent to a power generation device, and the power generation device generates power using the received feed water.

According to the steam generator described in the above (26), the heat of the feed water can be effectively utilized to extract power, and the efficiency of the plant can be improved.

(27) In some embodiments, in the steam generator described in any one of the above (18) to (26), the steam generator sends the whole amount of the water heated by the second carbon device to the The first evaporator or at least one of the high temperature heat exchangers (30, 31) heated to a temperature higher than the saturation temperature corresponding to the vapor pressure of the first evaporator.

According to the steam generator described in the above (27), the feed water heated by the second carbonizer that directly sends the feed water to the first evaporator is not sent to various heat utilization equipment for utilization of lower-temperature heat, but It is sent to at least one of the first evaporator or a high temperature heat exchanger heated to a higher temperature than the saturation temperature of the vapor pressure corresponding to the first evaporator, thereby reducing the amount of feed water heated by the second section carbonizer traffic. In this way, the temperature distribution of the feed water flowing in the carbon economizer can be made close to a better temperature distribution, the slope of the line corresponding to the feed water of the second carbon economizer on the TQ diagram increases, and the feed water supplied to the first evaporator can be increased. The temperature is close to the saturation temperature corresponding to the vapor pressure of the first evaporator, which can improve the heat utilization efficiency.

(28) An exhaust heat recovery plant (200) according to an embodiment of the present invention includes: the steam generator (6) according to any one of the above (1) to (27); and the steam generator using the above-mentioned steam generator The steam utilization device (100) of the generated steam.

According to the exhaust heat recovery plant described in the above (28), since the steam generator of any one of the above (1) to (27) is provided, the size of the carbon economizer (the size of the first carbon economizer and the size of the carbon economizer) can be suppressed. The total size of the two carbon sections) can be increased in size, and the efficiency of heat utilization of the heat medium can be improved by using the flash tank. Thereby, the enlargement of the exhaust heat recovery plant can be suppressed, and the heat utilization efficiency of the exhaust heat recovery plant can be improved.

(29) The compound factory (2) related to one embodiment of the present invention is provided with: The exhaust heat recovery plant described in the above (28), and the prime mover (4), the boiler or the fuel cell; the aforementioned steam utilization equipment includes steam turbines (102, 104, 106); the aforementioned heat medium is the exhaust gas of the aforementioned prime mover, the aforementioned exhaust gas of the aforementioned boiler gas or the exhaust gas of the aforementioned fuel cell.

According to the steam generator described in the above (29), the heat energy of the exhaust gas of the prime mover, the exhaust gas of the boiler, or the exhaust gas of the fuel cell can be efficiently recovered by the exhaust heat recovery plant. In addition, the wettability of the downstream section of the steam turbine can be reduced, and the corrosion of the turbine airfoil can be suppressed, and the efficiency of the steam turbine can be improved.

(30) A steam-electricity cogeneration plant (2) according to an embodiment of the present invention includes the exhaust heat recovery plant described in (28) above, a prime mover (4), a boiler or a fuel cell; the steam utilization facility is The steam is used as a heat source, and the heat medium is the exhaust gas of the prime mover, the exhaust gas of the boiler, or the exhaust gas of the fuel cell.

According to the steam generator described in the above (30), the heat energy of the exhaust gas of the prime mover, the exhaust gas of the boiler, or the exhaust gas of the fuel cell can be efficiently recovered by the exhaust heat recovery plant. Furthermore, by utilizing the steam generated by the steam generator as a heat source, a steam-electricity cogeneration plant with high heat utilization efficiency can be realized.

(31) Exhaust heat recovery related to one embodiment of the present invention A method for remodeling a plant, comprising the steps of increasing the number of carbon economizers (22, 24, 25) disposed on the downstream side of the first evaporator (26) in the heat medium flow path (18) to two or more, and The step of connecting the water supply pipeline (52, 27) and the flash tank (8), the water supply pipeline connects the adjacent one of the above two or more carbon economizers to the carbon economizer.

According to the modification method of the exhaust heat recovery plant described in the above (31), the size of the carbon economizer can be suppressed compared with the case where the temperature of the feed water is close to the saturated steam temperature with one economizer (the size of the first economizer). The size of the carbon device in the second section) can be increased, and the heat utilization efficiency of the heat medium can be improved by using a flash tank.

(32) A steam generating method according to an embodiment of the present invention, comprising: supplying the water heated by the first carbon block (22) provided in the heat medium flow path (18) to the heat medium flow path The step of providing the second carbon block (24) on the upstream side of the first carbon block in the flow direction of the heat medium; the water heated by the second carbon block is supplied to the heat medium flow path. In the flow direction of the heat medium, the first evaporator (26) is provided on the upstream side of the second carbon section, and the water heated by the first carbon section is connected to the first section carbon device by self-connection. The second water supply pipeline (53, 75, 77) branched from the first water supply pipeline (52, 27) of the carbon device in the second section above is supplied to the heat utilization equipment (8, 51, 61, 120, 122, 129, 130, 132).

According to the steam generating method described in the above (32), from the first The water heated by the carbon economizer is supplied to the heat utilization equipment through the second water supply pipeline that is branched from the first water supply pipeline connecting the first carbon device and the second carbon device. The flow rate of the second carbon device is higher than The flow rate of the 1st carbon device is reduced. Therefore, even if the feed water flow rate of the first stage carbonizer increases according to the flow rate of the feedwater supplied to the heat utilization equipment, the temperature of the feed water can be efficiently approached to the saturated steam temperature with the smaller second stage carbonizer. Therefore, the size of the carbon economizer (the sum of the size of the 1st economizer and the size of the 2nd economizer) can be suppressed from increasing in size compared with the case where the temperature of the feed water is made closer to the saturated steam temperature by one economizer , you can use heat utilization equipment to improve the heat utilization efficiency of the heat medium.

2(2A): Compound Factory

4: Gas Turbine

5: Exhaust heat recovery boiler

6(6A): Steam generating device

8: Flash tank

9: Chimney

12: Compressor

14: Burner

16: Turbine

18: Exhaust gas flow path

19: Generator

20: Heat Exchanger

22: 1st low pressure carbon saver

24: 2nd low pressure carbon saver

26: Low pressure evaporator

28: Low pressure superheater

30: 1st high pressure carbon saver

32: Medium pressure evaporator

34: Medium pressure superheater

36: 2nd high pressure carbon saver

38: High pressure evaporator

40: 1st high pressure superheater

42: 1st reheater

44: 2nd high pressure superheater

46: 2nd reheater

48, 52, 53, 54, 60: Water supply lines

50: Condensate pump

51: Condensate line

55, 65, 77: Feed valve

56, 57, 58: Vapor Lines

59: Pressure reducing valve

61: Feed water pump

62: Medium pressure feed pump

64,70,74,76: Water supply lines

72: High pressure feed pump

78,80: Vapor Lines

81,83: Desuperheater

82: Reheat steam line

97: Vapor Line

98: Reheat steam line

100: Steam Turbine Systems

102: High Pressure Steam Turbines

104: Intermediate pressure steam turbines

106: Low Pressure Steam Turbines

108: Condenser

110: Medium pressure exhaust line

112: Low pressure exhaust line

114: High pressure exhaust line

200: Exhaust heat recovery plant

205, 206: Flow adjustment valve

Claims (28)

A steam generating device is provided with: a heat medium flow path for supplying a heat medium to flow; a first carbon blocker arranged in the heat medium flow path; The second carbon insulator on the upstream side of the first carbon insulator; the first evaporator installed on the upstream side of the second carbon insulator in the flow direction of the heat medium in the heat medium flow path; The water heated by the charcoal in the first section is supplied to the first water supply pipeline formed by the method of the carbon in the second section; and branched from the first water supply pipeline to supply the water heated by the carbon in the first section The second water supply line formed by the way to the heat utilization equipment; the heat medium flow path is provided with a plurality of evaporators including the first evaporator; the first evaporator is in the plurality of evaporators. The flow direction of the heat medium flow path is located at the most downstream evaporator. The steam generator according to claim 1, wherein the heat utilization device is a first flash tank for generating flash steam. The steam generator according to claim 1 or claim 2, further comprising: a third water supply line for supplying the water heated by the second carbonizer to the first flash tank; The water supply line for supplying water to the aforementioned first carbon tank is branched to supply water to the aforementioned first flash tank. At least one of the fourth water supply lines constituted by the method. The steam generator according to claim 1 or 2, further comprising: a first steam line for supplying the steam generated in the first flash tank to a facility utilizing the steam; and a first steam line provided in the first The steam line is a superheater for superheating the steam generated in the first flash tank. The steam generator according to claim 1 or 2, wherein the steam generator includes a plurality of flash tanks including the first flash tank; and the pressures of the plurality of flash tanks are set to different pressures from each other. The steam generating apparatus according to claim 5, further comprising: a discharge water line connected in series to the plurality of flash tanks for the flow of the discharge water discharged from each of the flash tanks; The water heated by the boiler or the above-mentioned Section 2 carbon boiler is supplied to the 5th water supply line of the above-mentioned discharge water pipeline; the temperature of the water in the above-mentioned 5th water supply line is relatively corresponding to the above-mentioned plurality of flash tanks in the above-mentioned discharge water line. The flow direction of the flash tank is located on the upstream side of the position where the discharge water line is connected to the fifth feed water line, and the saturation temperature of the pressure is lower than that in the plurality of flash tanks corresponding to the flow in the discharge water line. Saturation of the pressure of the flash tank located on the downstream side of the point where the discharge water line is connected to the fifth feed water line higher temperature. The steam generating device according to claim 1 or 2, wherein the steam generating device is on the downstream side of the first evaporator in the flow direction of the heat medium in the heat medium flow path, and includes the steam generating device containing the first evaporator. A carbon economizer and a plurality of carbon economizers of the aforementioned second carbon economizer; constituted by using a part of the water from the outlet of at least one of the foregoing plurality of carbon economizers as a heat source . The steam generating device according to claim 1 or 2, wherein the steam generating device is on the downstream side of the first evaporator in the flow direction of the heat medium in the heat medium flow path, and includes the steam generating device containing the first evaporator. A carbon economizer and a plurality of carbon economizers of the aforementioned second carbon economizer; using a part of the water flowing in the water supply line connected to the inlet of at least one of the foregoing plurality of carbon economizers as a cooling medium It is composed of the way of utilizing and recovering the exhaust heat. A steam generating device is provided with: a heat medium flow path for supplying a heat medium to flow; a carbon economizer arranged in the heat medium flow path; The first evaporator on the upstream side of the evaporator; the first flash tank for generating flash steam; the first water supply line formed by supplying the water heated by the carbon economizer to the first evaporator; A second water supply line that is branched from the first water supply line to supply the water heated by the carbon economizer to the first flash tank; 2 The water flowing in the water supply line superheats the steam generated by the first flash tank; the steam generated by the flash evaporation of the water heated by the carbon economizer is used as the steam produced by the aforesaid flash before flashing. The water heated by the carbon economizer is superheated. The steam generator according to claim 1, 2 or 9, wherein the steam generator adjusts the flow rate of the feed water supplied to the first flash tank by adjusting the opening degree of a valve provided in the second feed water line . The steam generating device according to claim 1, 2 or 9, wherein the steam generating device adjusts the opening degree of a valve provided on the pipeline for flowing the discharge water of the first flash tank, or the steam generating device for the first flash tank. 1. Adjust the liquid level of the first flash tank by adjusting at least one of the flow rates of the pumps provided on the pipeline where the discharge water of the flash tank flows. The steam generating device according to claim 1, wherein the heat utilization device exchanges heat between the heated medium and the water heated by the first carbon heater, or heats the heated medium with the water heated by the first carbon heater. The heated water is mixed to heat the aforementioned heated medium. The steam generator according to claim 12, wherein the heated medium is 100°C or lower. The steam generating device of claim 1, wherein The heat utilization equipment exchanges heat between the cooling medium and the water heated by the first carbonizer, cools the cooling medium, and further heats the water heated by the first carbonizer. The steam generating device according to claim 14, wherein the heat utilization equipment heats the water heated by the carbon heater in the first section to a temperature higher than 100°C. The steam generating device according to claim 14 or claim 15, wherein the flow direction of the heat medium in the heat medium flow path of the steam generating device is more downstream than the first evaporator, and the steam generating device contains the first section. Carbon saver and a plurality of carbon savers of the above-mentioned second carbon saver; among the plurality of carbon savers, the carbon saver disposed most upstream in the flow direction of the heat medium in the heat medium flow path will be heated The feed water is supplied to the first evaporator; the heat utilization device cools the cooling medium to a temperature below the saturation temperature corresponding to the vapor pressure in the first evaporator. A steam generating device is provided with: a heat medium flow path for supplying a heat medium to flow; a first carbon blocker arranged in the heat medium flow path; The second carbon separator on the upstream side of the first carbon separator; the first evaporator provided on the upstream side of the second carbon separator in the flow direction of the heat medium in the heat medium flow path; The water heated by the carbon device in the first section is supplied to the first water supply pipeline in the manner in which the carbon device in the second section is supplied, and the water heated by the carbon device in the second section is not mixed with the heat medium. The 6th water supply pipeline formed by the way of heat exchange and supply to the above-mentioned first evaporator; the mass flow rate of the feed water flowing to the above-mentioned second section carbon container is smaller than that of the feed water flowing to the above-mentioned first section carbon container; the above-mentioned steam The flow direction of the heat medium in the heat medium flow path of the generating device is further downstream than the first evaporator, and includes a plurality of carbon economizers including the first carbon economizer and the second carbon economizer; and A water supply line that obtains a part of the water from the outlet of one carbon economizer among the plurality of carbon economizers. The steam generating device according to claim 17, wherein the steam generating device includes a third carbon segment in the flow direction of the heat medium in the heat medium flow path more downstream than the second carbon segment; The mass flow rate of the feed water to the aforesaid section 2 carbon container is less than the mass flow rate of the feed water flowing through the aforesaid section 3 carbon container. The steam generator according to claim 17, wherein the steam generator includes two or more feed water acquisition lines for acquiring a part of the water from the outlets of the different carbon economizers, respectively. The steam generating device according to claim 17 or claim 18, wherein the steam generating device is located on the downstream side of the flow direction of the heat medium in the heat medium flow path than the first evaporator, and includes the steam generating device containing the first evaporator. A carbon economizer and a plurality of carbon economizers of the second carbon economizer; and a feed water supply line for supplying feed water to an inlet of one of the plurality of carbon economizers. The steam generating device of claim 17, wherein The steam generator is provided with a feed water supply line for supplying feed water to the inlet of one carbon economizer among the plurality of carbon economizers. The steam generator according to claim 20, wherein the steam generator includes two or more feed water supply lines for supplying feed water to different inlets of the carbon economizers, respectively. The steam generating device according to claim 20, wherein the feed water supply line supplies feed water with a lower temperature than the feed water outlet of the carbon economizer to which the water is supplied, and the supply temperature is set at a temperature higher than that of the flow direction of the heat medium. The carbon economizer to which the feed water is supplied has a higher feed water inlet than the carbon economizer downstream. The steam generating device according to claim 17, wherein the steam generating device is further provided with a power generating device for sending the feed water obtained from at least one of the feed water obtaining pipelines to the power generating device, and the power generating device uses the received feed water to generate power. The steam generating device according to claim 17 or 18, wherein the steam generating device sends the whole amount of the water heated by the second carbon heater to the first evaporator, or to the first evaporator heated to a temperature more corresponding to the aforementioned At least one of the high-temperature heat exchangers having a higher temperature than the saturation temperature of the vapor pressure of the first evaporator. An exhaust heat recovery plant comprising: the steam generating device described in any one of claim 1 to claim 25; and a steam utilization facility for utilizing the steam generated by the steam generating device. A compound plant, comprising: the exhaust heat recovery plant described in claim 26, and a prime mover, a boiler, or a fuel cell; the steam utilization equipment includes a steam turbine; the heat medium is the exhaust gas of the prime mover and the exhaust gas of the boiler Gas or exhaust gas of the aforementioned fuel cell. A steam-electricity cogeneration plant, comprising: the exhaust heat recovery plant described in claim 26, and a prime mover, a boiler or a fuel cell; the steam utilization equipment is constituted by using the steam as a heat source; the heat medium is The exhaust gas of the prime mover, the exhaust gas of the boiler, or the exhaust gas of the fuel cell.

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